EP2815194A2 - Methods and systems for co2 condensation - Google Patents

Methods and systems for co2 condensation

Info

Publication number
EP2815194A2
EP2815194A2 EP12775386.1A EP12775386A EP2815194A2 EP 2815194 A2 EP2815194 A2 EP 2815194A2 EP 12775386 A EP12775386 A EP 12775386A EP 2815194 A2 EP2815194 A2 EP 2815194A2
Authority
EP
European Patent Office
Prior art keywords
stream
cooling
cooled
temperature
condensed
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.)
Pending
Application number
EP12775386.1A
Other languages
German (de)
French (fr)
Inventor
Miguel Angel Gonzalez Salazar
Vittorio Michelassi
Christian Vogel
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.)
General Electric Co
Original Assignee
General Electric Co
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 General Electric Co filed Critical General Electric Co
Publication of EP2815194A2 publication Critical patent/EP2815194A2/en
Pending legal-status Critical Current

Links

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
    • F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
    • 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
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0027—Oxides of carbon, e.g. CO2
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0225—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using other external refrigeration means not provided before, e.g. heat driven absorption chillers
    • 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
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/80—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/80—Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.
    • 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
    • F25J2270/908—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by regenerative chillers, i.e. oscillating or dynamic systems, e.g. Stirling refrigerator, thermoelectric ("Peltier") or magnetic refrigeration

Definitions

  • the present disclosure relates to methods and systems for carbon dioxide (CO?) condensation using magneto-caloric cooling. More particularly, the present disclosure relates to methods and systems for CO ; condensation in an intereooled compression and pumping train using magneto-caloric cooling.
  • CO carbon dioxide
  • a method of condensing carbon dioxide (CO 2 ) from a CO 2 stream includes (i) compressin and cooling die COj stream to form a partially cooled CO> stream, wherein the partially cooled C0 2 stream is cooled to a .first temperature.
  • the method includes (ii) cooling the partially cooled CO ? ; stream to a second temperature by magneto-caloric cooling to form a cooled CO 2 stream.
  • the method further inciudes (in) condensing at least a portion of C ⁇ 3 ⁇ 4 in the cooled CO stream at ihe second temperature to form a condensed CO? stream.
  • a method o condensing carbon dioxide (CO 2 ) from a C ⁇ 3 ⁇ 4 stream includes (i) cooling the CO ? stream in a first cooling stage comprising a first heat exchanger to form a first partially cooled CO?, stream.
  • the method further includes (ii) compressing the first partially cooled COj stream to .form a first compressed CO? stream.
  • the method further includes (Hi) cooling the first compressed CO 2 stream in a second cooling stage comprising a second heat exchanger to form a second partially cooled CO ? stream.
  • the method further inciudes (iv) compressing the second partially cooled CO? stream to .form a second compressed CO? stream.
  • the method further includes (v) cooling the second compressed CO2 stream to a first temperature in a third cooling stage comprising a third heat exchanger to form a partially cooled CO? stream.
  • the method further includes (vi) cooling the partially coo!ed CO? stream to a second temperature by magneto-caloric cooling to form a cooled CO 2 stream.
  • the method further includes (vn) condensing at least a portion of CO ? in the cooied CO ? stream at the second temperature to form a condensed CO ? stream.
  • a system for condensing carbon dioxide (CO ? ) from a CO ? stream includes (t) one or more compression stages configured to receive the CO ? stream.
  • the system further includes (ii) one or more cooling stages in fluid communication with the one or more compression stages, wherein a combination of the one or more compression stages and the one or more cooling stages is configured to compress and cool the CO ? stream to a first temperature to form a parti all -cooied CO ? stream.
  • the system further includes (.Hi) a magneto-caloric cooling stage configured to receive the parti ally-cooled CO ? stream and cool the partially-cooled CO 2 stream to a second temperature to form a cooied CO ?
  • the system further includes (iv) a condensation stage configured to condense a portion of CO ? in the cooled CO ? stream at the second temperature, thereby condensing CO ? from the cooled compressed CO2 stream to form a condensed C ⁇ 3 ⁇ 4 stream.
  • FIG. 1 is a flow chart for a method of CO; condensation from a C ⁇ 3 ⁇ 4 stream, i accordance with one embodiment of the invention.
  • FIG. 2 is a flow chart for a melhod of C ⁇ 1 ⁇ 4 condensation from a C ⁇ 3 ⁇ 4 stream, i accordance with one embodiment of the invention.
  • FIG. 3 is a biock diagram of a system for CO? condensation from a
  • FIG. 4 is a biock diagram of a system for CO?, condensation from a
  • FIG. 5 is a biock diagram of a. system for CO? condensation from a
  • JG. 6 is a block diagram of a system for C0 2 condensation from a
  • J0O153 PIG- 7 is a biock diagram of a system for C0 2 condensation from a
  • CO> stream in accordance with one embodiment of the invention.
  • FIG. 8 is a block diagram of a system for CO? condensation from a
  • FIG. 9 is a biock diagram of a system for CO? condensation from a
  • FIG. 10 is a pressure versus temperature diagram for CO2
  • embodiments of the present invention include methods and systems suitable for CO> condensation.
  • liquefying and pumping of CO 2 may require high energy input.
  • a pressure o approximately 60 bar may be required to iiquefy CO 2 at 20 °C.
  • an intermediate magnetic cooling step advantageously lowers the C ⁇ 1 ⁇ 2 temperature to less than 0 *C, significantly reducing the required work of the overall system.
  • an overall efficiency improvement of about 10 percent to about 15 percent may be possible using the methods and systems described herein.
  • Approximating language may be applied to modify any quantitati e representation that could permissibly vary without resulting in a change in the basic function to which it is related. Accordingly, a value modified by a term or terms, such as "about”, is not limited lo the precise value specified. In some instances, the approximating language may correspond to the precision of an. instrument for measuring the value.
  • j ⁇ 223 i one embodiment, as shown in Figures ⁇ and 3, a method 10 for condensing carbon dioxide from a CO 2 stream i provided.
  • the term "C0 2 stream”, as used herein, refers to a stream of CO2 gas mixture emitted as a resul of the processing of fuels, such as. natural gas, bioroass. gasoline, diesel fuel coal, oil shale, fuel oil, tar sands, and combinations thereof, hi some embodiments, the €X3 ⁇ 4 stream includes a C ⁇ 3 ⁇ 4 stream emitted from a gas turbine.
  • the CO? stream further includes one more of nitrogen, nitrogen dioxide, oxygen, or water vapor.
  • the CO 2 stream further includes impurities or pollutants, examples of which include, but are not limited to, nitrogen, nitrogen oxides, sulfur oxides, carbon monoxide, hydrogen sulfide, un burnt hydrocarbons, particulate matter, and combinations thereof, in particular embodiments, the CO? stream is substantially free of the impurities or pollutants, in particular embodiments, the CO-> stream essentially includes carbon dioxide.
  • CO 2 stream is less than about 50 mole percent, in some embodiments, the amount of impuriiies or polliitants in the CO: stream is less than about 20 mole percent. In some embodiments, the amount of impurities or pollutants in the CO? stream is in a range .from about 10 moie percent to about 20 mole percent. .In some embodiments, the amount of impurities or polliitants in the C0 2 stream is less than about 5 mole percent.
  • the method includes receiving a CO 2 stream 101 , as indicated in Fig. 3, from a hydrocarbon processing, combustion, gasification or a similar ' power plant (not shown). As indicated in Figures 1 and 3, at step 1.1, the method 1.0 includes compressing and cooling the CO 2 stream 101 t form a partiall cooled O2 stream 201.
  • the CO-> stream 301 may be compressed using or more compression stages 120.
  • the CO ; j stream may be cooled using or more cooling stages 1.10.
  • the CO stream 101 may be compressed to a desired pressure by using one or more compression stages, as indicated by 1 20 in Fig, 3.
  • the compression stage 120 may further include one or more compressors, such as, 121 and 1 22, in some embodiments, it should be noted that in Fig. 3, the two compressors 1 25 and 1 22 are shown as an exemplars' embodiment only and the actual number of compressors and their individual configuration may vary depending on the end result desired.
  • the C > stream 101 may be conipressed to a pressure and temperature desired for the magnetic cooling and condensation steps 12 and 13, respectively.
  • the C ⁇ 3 ⁇ 4 stream 101 may be compressed to a pressure in a range from aboul 10 bar io about 60 bar prior to the magnetic cooling step 12.
  • the CO? stream 101 may be compressed to a pressure in a range from about 20 bar to about 40 bar prior to the magnetic cooling step 12.
  • the COj stream 101 may be cooled to a desired temperature by using one or more cooling stages, as indicated by 1 10 in Fig. 3.
  • the cooling stage 1 10 may further include one or more heat exchangers, such as, 1 i L 112 and 1 1 3, in some embodiments.
  • the three heat exchangers 111 , 112, and 1 13 are shown as an exemplar? embodiment only and the actual number of heat exchangers id their individual configuration may vary depending on the end result desired.
  • one or more of the heat exchangers may be cooled using a cooling medium.
  • one more of the heat exchangers may be cooled using cooling air, cooling water, or both, as indicated by 1 15 in Fig. 3.
  • the cooling stage may further include one or more intereoolers to cool the exhaust gas stream 1 1 without affecting the pressure.
  • cooling stage 1 10 and compression stage 120 is shown as mi exemplary embodiment only and the actual configuration may vary depending on the end result desired.
  • the method may include cooling the CO 2 stream in a heal exchanger 1 1 1 prior to compressing the CC3 ⁇ 4 stream in a compressor 121. (not shown).
  • the method further includes cooling the CO? stream 101 to a first temperature by expanding the CO3 ⁇ 4 stream in one or more expanders 123, a indicated in Fig. 8.
  • the method includes an expansion step that decreases the pressure of the CO? stream 10 i from absolute pressure levels greater than about 20 bar to pressure levels of around 20 bar, thereby decreasing ihe temperature of the C ⁇ 3 ⁇ 4 stream 101 to values iower than that may be reached by air or water cooling.
  • the expansion step it is believed that by employing the expansion step, the overall duty of the magneto-caloric cooling step 12 may be reduced, as the inlet temperature of the partially -cooled CO? stream to the magneto-caloric step may be lower than thai without an expansion step.
  • the work extracted in the expansion step may be further used for the .magneto-caloric cooling step 12.
  • the C ⁇ 3 ⁇ 4 stream .101 may be cooled to a temperature and pressure desired for the magnetic cooling and condensation steps 12 and 13.
  • the method includes compressing and cooling the CO?, stream 101 to form a partially cooled CO? stream 201, as indicated in Fig. 3.
  • the method further includes cooling the COj ⁇ stream 10 i to a first temperature by expanding the CO* stream in one or more expanders 123 to form the partially cooled C0 2 . stream 201, as indicated in Fig. 8.
  • the method includes cooling the partially cooled
  • the partially cooled CO? stream 201 may be cooled to a temperature in a range from about 5 degrees Celsius lo about 35 degrees Celsius, prior to the magnetic cooling step 12.
  • the partially cooled CO stream .201 may be cooled to a temperature in a range from about 10 degrees Celsius to about 25 degrees Celsius, prior to the magnetic cooling step 12.
  • the condensation temperature is determined by the temperature of the cooling medium, which can be cooling water or air. As shown in Fig. 10, at a condensation temperature in a range from about 20 degrees Celsius to about 25 degrees Celsius, an absolute pressure of approximately 60 bar is required to liquefy CO ? . In contrast, by cooling the CO? stream to a. temperature in a range from about -25 degrees Celsius to about 0 degrees Celsius, lower pressure may be advantageously used for condensing C ⁇ 3 ⁇ 4 from the partially cooled COi stream 201.
  • the .method further includes, at step 12, cooling the partially cooled CO 2 stream 201 to a second temperature by magneto-caloric cooling to form a cooled CO 2 stream 302. as indicated in Figures 1 and 3.
  • the method includes cooling the partiaily-cooled CO ? stream 201 using a .magneto-caloric cooling stage 200, as indicated in Fig. 3,
  • a magneto-caloric cooling stage 200 includes a heat exchanger 212 and an externa! magneto-caloric cooling device 21 1.
  • the magneto-caloric cooling device 21 1 is configured to provide coohng to the heat exchanger 212, as shown in Fig. 3.
  • the magneto-caloric cooling device 21 1 includes a cold and a hot heat exchanger, a permanent magnet assembly or an induction coil magnet assembly, a regenerator of magneto-caloric material, and a heat transfer fluid cycle.
  • the heat transfer fluid is pumped through the regenerator and the heal exchanger by a fluid pump (not shown).
  • the magneto-caloric cooling devices works on an active magnetic regeneration cycle (AMR) and provides cooling power to a heat transfer fluid by sequential magnetization and demagnetization of the magneto-calorie regenerator with flow reversal heat transfer flow.
  • AMR active magnetic regeneration cycle
  • the sequential magnetizatio and demagnetization of the magneto-caloric regenerator may be provided for by a rotaiy set-up where the regenerator passes through a bore of the magnet system.
  • the sequential magnetization and demagnetization of the magneto-caloric regenerator may be provided for by a reciprocating linear device.
  • An exemplary magnet assembly and magneto-caloric cooling device are described in US Patent Application Serial No.
  • the heat at the hot heat exchanger may be delivered to the ambient environment
  • the heal at the hot heat exchanger may be delivered to the return ilovv of the condensed and liquefied C ⁇ 3 ⁇ 4 after the pumping of the liquid C ⁇ 3 ⁇ 4, as described herein later.
  • the magneto-caloric cooling stage further includes a heat exchanger 212.
  • the magneto-caloric cooling device 21 1 is configured to provide cooling to the heat exchanger 212.
  • the heat exchanger 212 is in fluid communication with the one or more cooling stages i 10 and the one or more compression stages 120.
  • the heat exchanger 212 is in fluid communication with the partially cooled Ci3 ⁇ 4 stream 201 generated after the compression and cooling step 1 1 .
  • the magneto-caloric cooling device 21 1 is configured to provide cooling to the heat exchanger 212 such thai the partially cooled C0 2 .
  • stream 2 1 is cooled to the second temperature.
  • the second temperature is in a range of from about 0 degrees Celsius to about-25 degrees Celsius. In one embodiment, the second temperature is in a range of from about 5 degrees Celsius to about-20 degrees Celsius.
  • the step 13 of cooling the partially-cooled CO;> stream in the magneto-caloric cooling stage results m a cooled C0 2 stream.
  • the magneto-caloric cooling device 21 1 is configured to provide cooling to ihe heat exchanger 212 such that the partially cooled C0 2 stream 20 i is cooled to the second temperature, such that CO,; condenses from the cooled CO ? stream.
  • the method includes compressing the CC stream 101 to a pressure in a range from about 20 bar to about 40 bar, in some embodiments. As indicated i Fig. 10, at a pressure level of 40 bar, the CC>> condenses at a temperature of 5 C. Further, as indicated in Fig. 10, at a pressure level of 20 bar. the Ct condenses at a temperature of -20 C.
  • the method further includes, at step 13. condensing at least a portion of C ⁇ 3 ⁇ 4. in the cooled CO 2 stream at the second temperature, thereby condensing CO? from the cooled CO? stream to form a condensed CO ? stream 302.
  • the method includes condensing at least portion of CO2 in the cooled CO2 stream at a pressure in a range of from about 20 bar to about 60 bar.
  • the method includes condensing at least a portion of CO2 in the cooled CO?, stream at a pressure in a range of from about 20 bar to about 40 bar. Accordingly, the method of the present invention advantageously allows for condensation of CO ? at a lower pressure, in some embodiments.
  • the method includes performing the steps of cooling the partially cooled CO ? stream to form a cooled CO ? stream ⁇ 2 and condensing CO2 from the cooled CO;? stream 13 simultaneously.
  • the method includes performing the steps of cooling the partially cooled CO2 stream to form a cooled C ⁇ 3 ⁇ 4 stream 1 2 and condensing CO2 from the cooled CO2 stream 13 sequentially.
  • a cooled CO 2 stream may be generated from the partially cooled O? stream 201 in the heat exchanger 212.
  • a portion of CO2 from the cooled CO? stream condenses in the heat-generator itself forming a condensed CO ? stream 302, as indicated in Fig. 3.
  • a cooled CO ? , stream 301 is generated from the partially cooled CO ? , stream 201 in the heat exchanger 212.
  • the method further includes transferring the cooled CO 2 stream 3 1. to a condenser 213, as indicated in Fig. 4, in such embodiments, a portion of CO 2 f om the cooied CO ? stream 301 condenses in the condenser 213 and forms a condensed CO ; stream 302, as indicated it) Fig. 4.
  • the method includes condensing at least about
  • the method includes condensing at least about 90 weight percent of CO2. in the Ct1 ⁇ 4 stream 101 to form the condensed CO? stream 302. In some embodiments, the method includes condensing 50 weight percent to about 90 weight percent of CO ? in the CO ? stream 101 to form the condensed CO ? stream 302. In some embodiments, the method includes condensing at least about 99 weight percent of CO ? in the CO? stream 1 0. ⁇ to form the condensed CO ? stream 302. j . 00 6] In some embodiments, as noted earlier, the CO 2 stream 101 further includes one or more components in addition to carbon dioxide.
  • the method further optionally includes generating a lean stream (indicated by doited arrow 202) after the steps of magneto-caloric cooling (step 12) and CO 2 condensation (step 1.3).
  • the term "lean stream" 202 refers to a siream in which the CO.; content is lower than that of the CO 2 content in the CO.; stream. 101.
  • almost all of the CO 2 in the CO ? stream is condensed in the step 13.
  • the lean CO2 stream is substantially free of CO?,
  • a portion of the CO2 stream may not condense in the step 13 and the lean stream may include uncondensed CO2 gas mixture,
  • the lean stream 202 may include one or more non-condensable components, which may not condense i the step 13.
  • the lean stream 202 may include one or more liquid components.
  • the lean stream may be further configured to be in fluid communication with a liquid-gas separator.
  • the lean stream 202 may include one or more of nitrogen, oxygen, or sulfur dioxide.
  • the method may further include dehumidilying the CO 2 stream 101 before step 1 1.
  • the method may further include dehumidtfying the partially cooled CO? stream 201 after step I I and before step 1 2.
  • the system 1 00 may further include a dehumidifier configured to be in flow communication (not. shown) with the CO ? siream 101.
  • the system 100 may further include a dehumidifier configured to be in flow communication ⁇ not shown) with the CO 3 stream 101.
  • the method further includes circulating the condensed CO 2 stream 302 to one or more cooling stages used for cooling the CO? stream. As indicated in Fig, 5, the method further includes Circulating the condensed CO 2 stream to a heal exchanger 1 13 via a circulation loop 303. In such embodiments, the method further includes a recuperation step where the condensed COj stream is circulated back to further cool the partially cooled CO ? stream 201 before the magnet o-caioric cooling step 12, in some embodiments, the recuperation step may increase the efficiency of the magneto-caloric step.
  • the recuperation of condensed CO?, stream to the heat exchanger 113 may result in cooling of the partially cooled CO 2 stream 201 below the temperature required for condensation of CO 2 .
  • the method may further include condensing the CO ? , in the partially cooled CO? stream 20.1 to form a recuperated condensed CO2 stream 501 , as indicated in Fig. 5.
  • the method .further includes increasing a pressure of the condensed C O.. stream 302 using a pump 300. as indicated in Fig, 3.
  • the method may further include increasing a pressure of the recuperated condensed CO2 stream 50.1 using a pump 300. as indicated in Fig. 5.
  • the method includes increasing a pressure of the condensed C ⁇ 1 ⁇ 4 stream 302 or the recuperated condensed CO2 stream 502 to a pressure desired for CO2 sequestration or end -use.
  • the method includes increasing pressure of the condensed CO 2 stream 302 or the recuperated condensed CO2 stream 502 to a pressure in a range from about 150 bar to about 180 bar,
  • the method further includes generating a pressurized CO ? , stream 401 after the pumping step. In some embodiments, the method further includes generating a supercritical CO? stream 401 after the pumping step. In some embodiments, as noted earlier, the pressurized CO stream 401 may be used for enhanced oil recovery, CO storage, or CO 2 sequestration.
  • the system 100 includes one or more compression stages 120 configured
  • the system i 00 further includes one or more cooling stages 1 10 in fluid communication with the one or more compression stages 120.
  • a combination of the one or more compression stages .120 and the one or more cooling stages 1 1 is configured to compress and cool the CO 2 stream 101 to a first temperature lo form a partially-cooled CO ? ; stream 201.
  • the system 100 further includes a magneto-caloric cooling stage 200 configured to receive the partially-cooled € ( 3 ⁇ 4, stream 201 and coo! the partially-cooled CO 2 stream 201 to a second temperature to form a cooled CO> stream 301.
  • the magneto-caloric cooling stage 200 further includes a heat exchanger 212, wherein the magneto-caloric cooling device 21 1 is configured to provide cooling to the heat exchanger 212.
  • the heat exchanger 21 2 is in fluid communication with the one or more cooling stages 1 1 and the one or more compression stages 120.
  • the heat exchanger 212 is configured to condense a portion of CO 2 in the partially cooled CO 2 stream 201 to form the condensed CO2 stream 302.
  • the system 100 further includes a condensation stage 213 configured to condense a portion of C ⁇ 1 ⁇ 4 in the cooled CO 2 stream 301 at the second temperature, thereby condensing CO 2 from the cooled CO 2 stream 301 to form a condensed CO 2 stream 302.
  • the system 100 further includes a pump 300 configured io recei ve the condensed CO 2 stream 302 and increase the pressure of the condensed CO 2 stream 302.
  • the system further includes a circulation loop 303 configured to circulate a portio of the condensed C ⁇ 3 ⁇ 4 stream 302 to the one or more cooling stages 1 10.
  • a meihod 20 of condensing carbon dioxide from a CO 2 stream 1 01 is provided.
  • the method includes, at step 21 , cooling the CO stream 101 in a first cooling stage including a first heat exchanger 111 to form a first partially cooled CO? stream 102.
  • the method includes, at step .2.2. compressing the ⁇ first partially cooled C0 2 stream 102 in a first compressor 1 21 to form a first compressed CO? stream 103.
  • the method includes, at step 23, cooling the first compressed CO;? stream 103 in a second cooling stage including a second heat exchanger 1 1.2 to form a second partially cooled COi stream 104.
  • the method includes, at step 24, compressing the second partially cooled CO? stream " 104 in a second compressor 122 to form a second compressed CO; stream 105.
  • the method includes, at step 25, cooling the second compressed CO? stream 105 to a first temperature in a third cooling stage comprising a third heat exchanger 1 1.3 to form a partiall cooled COj> stream 2 1.
  • the method 20 includes, at step 26, cooling the partially cooled CO.; stream 201 to a second temperature fay magneto-caloric cooling using a magneto-caloric cooling stage 200 to form a cooled CO? stream (not shown).
  • a magneto-caloric cooling stage .200 includes a heat exchanger 212 and an external magneto-caloric cooling device 21.1.
  • the magneto-caloric cooling device 211 is configured to provide cooling to the heat exchanger 212. as indicated in Fig, 3.
  • the method includes, at step 27, condensing at least a portion of CO? in the cooled CO siream at the second temperature, thereby condensing C ⁇ 3 ⁇ 4 from the cooled CO? stream to form a condensed C ⁇ 3 ⁇ 4 stream 302.
  • a cooled CO? stream is generated from the partially cooled CO? stream 20.1 in the heal exchanger 212.
  • a portion of CO2 from the cooled CO? stream condenses in the heat-generator itself .forming a condensed C ⁇ 3 ⁇ 4 stream 302, as indicated in fig. 3.
  • the method further includes increasing a pressure of the condensed CO? stream 302 using a pump 300, as indicated in Fig. 3.
  • the method further includes generating a pressurized CO , stream 401 after the pumping step, in some embodiments, as noted earlier, the pressurized CC stream 401 may be used for enhanced oil recover y -, CO ? storage, or C0 2 sequestration.
  • a method and a system for condensing CO 2 from a CO 2 stream 101 is provided.
  • the method and system is similar to the system and method illustrated in Fig. 3. with the addition that the method further includes transferring the cooled CO ; j stream 301 to a condenser 213, as indicated in Fig. 4.
  • a portion of CO ; from the cooled CO2 stream 301 condenses in the condenser 213 and forms a condensed C ⁇ 3 ⁇ 4 stream 302, as indicated in Fig. 4.
  • a method and system for condensing CO;? from a CO ? stream 101 is provided.
  • the method and system is similar to the system and method illustrated in Fig. 3. with the addition that the method further includes circulating a portion of the condensed CO2 stream 302 to the third heat exchanger 113 via a circulation loop 303.
  • the recuperation of condensed CO 2 stream to the heat exchanger 1 13 may result in cooling of the second compressed CO2 stream 105 below the temperature required for condensation of CO ⁇ .
  • the method may further include condensing the CO 2 in the second compressed CO;? stream 105 to form a recuperated condensed CO 2 stream 501 , as indicated in Fig. 5.
  • a method and s stem for condensing O> from a CO 2 stream 101 is provided.
  • the method and system is similar to the system and method illustrated in Fig. 4. with the addition that the method further includes circulating a portion of the condensed CO ? stream to the third heat exchanger 113 via a circulation loop 303.
  • the recuperation of condensed CO 2 to the heat exchanger 113 may result in cooling of the second compressed CO 2 stream 105 helow the temperature required for condensation of CO ?
  • the method may further include condensing the COj in the second compressed CO3 stream 105 to form a recuperated condensed CO2 stream 501.
  • a method mid a system for condensing CO? from a CO 2 stream 101 is provided.
  • the method and system is similar to (he system and method illustrated in Fig. 3. with the addition that the method further includes circulating a portion, of the pressurized C ⁇ 3 ⁇ 4 stream 401 to the third heat exchanger 113 via a circulation !oop 403.
  • the recuperaiion of pressurized C ⁇ 3 ⁇ 4. stream 401 to the third heat exchanger 1 1.3 may result in cooling of the second compressed C0 2 stream 1.05 below the temperature required for condensation of CO?, in some embodiments, the method may further include condensing the CO ?
  • a method id a system for condensing CO? from a 2 stream 101 is illustrated.
  • the method and system is similar to the system and method illustrated i Fig. 3, with the addition that the method further includes forming a third partially cooled CO2 stream 106 in the third heat exchanger 1 .
  • the method further includes cooling the third partially cooled CO : stream 106 to a first temperature by expanding the third partially cooled CO? stream 106 in one or more expanders 123, before the magneto-caloric cooling step, to form the parti all -cooled CO?, stream 201 , as indicated i Fig. 8.
  • a method and a system for condensing CO 2 from a CO? stream 101 is illustrated.
  • the method and system is similar to the system and method illustrated in Fig. 8, with the addition that the third cooling stage further comprises a fourth beat exchanger 114, and the method further includes circulating a portion of the pressurized CO 2 stream 401 to the fourth heat exchanger 1 14 via a circulation loop 403.
  • the .method further includes forming a fourth partially cooled C ⁇ 3 ⁇ 4 stream 107 after the expansion step and transferring the fourth partially cooled CO 2 stream 107 to the fourth heat exchanger 1 14.
  • stream 401 to the fourth heat exchanger 1 14 may result in cooling of the fourth partially cooled C0 2 stream 107 below the temperature required for condensation of CO?
  • the method may further include condensing the C ⁇ 1 ⁇ 4 in the fourth partially cooled CO.: stream 107 io form a recuperated condensed COj> stream 501, as ' indicated in Fig. 9.
  • the method reduces the penalty on the less- efficient COj compression step, in some embodiments, the method may reduce the overall penalty for C ⁇ . liquefaction and pumping by improving the efficiency of the compression and pumping system.
  • the magneto-caloric cooling stage may reduce the penalty by more than 10%.
  • the magneto-caloric cooling stage may reduce the penalty fay more than 20%.
  • the overall plant efficiency may be improved by using one or more of the method embodiments, described herein,
  • some embodiments of the invention advantageously allow for improved range of operabilify of CCb compression and liquefaction systems.
  • conventional CO;> compression mid iiquefaction systems the ambient temperature of the cooling air or cooling water may limit the range of operabiiity.
  • Supercritical CO 2 may not liquefy at temperatures greater than about 32 °C, the critical temperature of CO2.
  • the magnetic cooling step may advantageously allow cooling of CO.; to the sufacriticaS range, thereby enabling the operabiiity of the compression and liquefaction systems under any ambient conditions.

Landscapes

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

Abstract

In accordance with one aspect of the present invention, methods of condensing carbon dioxide (CO2) from a CO2 stream are provided. The method includes (i) compressing and cooling the CO2 stream to form a partially cooled CO2 stream, wherein the partially cooled CO2, stream is cooled to a first temperature. The method includes (ii) cooling the partially cooled CO2 stream to a second temperature fay magneto-caloric cooling to form a cooled CO2stream. The method further includes (iii) condensing at least a portion of CO2 in the cooled CO2 stream to form a condensed CO2 stream. Systems for condensing carbon dioxide (CO2) from a CO2 stream are also provided

Description

METHODS AND SYSTEMS FOR CO2 CONDENSATION
BACKGROUND
TECHNICAL FIELD
[0001] The present disclosure relates to methods and systems for carbon dioxide (CO?) condensation using magneto-caloric cooling. More particularly, the present disclosure relates to methods and systems for CO; condensation in an intereooled compression and pumping train using magneto-caloric cooling.
DISCUSSION OF RELATED ART
}00O2j Power generating processes thai are based on combustion of carbon containing fuel typically produce CO2 as a byproduct, it may be desirable to capture or otherwise separate the CO;> from the gas mixture to prevent the release of CO2 into the environment and/or to utilize CO; in the power generation process or in other processes. It may be further desirable to liquefy/condense the separated CO? to facilitate transport and storage of the separated CO2. CO2 compression, liquefaction and pumping trains may be used to liquefy CO;?, for desired end-use applications. However, .methods for condensation/liquefaction of CO- may be energy intensive.
]00O3| Thus, there is a need for efficient methods and systems for condensation of C<¼. Further, there is a. need for efficient methods and systems for condensation of CO > in inter cooled compression and pumping trains.
BRIEF DESCRIPTION
IOOO43 fa accordance with one aspect of the present invention, a method of condensing carbon dioxide (CO2) from a CO2 stream is provided. The method includes (i) compressin and cooling die COj stream to form a partially cooled CO> stream, wherein the partially cooled C02 stream is cooled to a .first temperature. The method includes (ii) cooling the partially cooled CO?; stream to a second temperature by magneto-caloric cooling to form a cooled CO2 stream. The method further inciudes (in) condensing at least a portion of C<¾ in the cooled CO stream at ihe second temperature to form a condensed CO? stream.
[OOOSi In accordance with another aspect of the present invention a method o condensing carbon dioxide (CO2) from a C<¾ stream is provided. The method includes (i) cooling the CO? stream in a first cooling stage comprising a first heat exchanger to form a first partially cooled CO?, stream. The method further includes (ii) compressing the first partially cooled COj stream to .form a first compressed CO? stream. The method further includes (Hi) cooling the first compressed CO2 stream in a second cooling stage comprising a second heat exchanger to form a second partially cooled CO? stream. The method further inciudes (iv) compressing the second partially cooled CO? stream to .form a second compressed CO? stream. The method further includes (v) cooling the second compressed CO2 stream to a first temperature in a third cooling stage comprising a third heat exchanger to form a partially cooled CO? stream. The method further includes (vi) cooling the partially coo!ed CO? stream to a second temperature by magneto-caloric cooling to form a cooled CO2 stream. The method further includes (vn) condensing at least a portion of CO? in the cooied CO? stream at the second temperature to form a condensed CO? stream.
[000 j In accordance with yet another aspect of the present invention, a system for condensing carbon dioxide (CO?) from a CO? stream is provided. The system includes (t) one or more compression stages configured to receive the CO? stream. The system further includes (ii) one or more cooling stages in fluid communication with the one or more compression stages, wherein a combination of the one or more compression stages and the one or more cooling stages is configured to compress and cool the CO? stream to a first temperature to form a parti all -cooied CO? stream. The system further includes (.Hi) a magneto-caloric cooling stage configured to receive the parti ally-cooled CO? stream and cool the partially-cooled CO2 stream to a second temperature to form a cooied CO? stream. The system further includes (iv) a condensation stage configured to condense a portion of CO? in the cooled CO? stream at the second temperature, thereby condensing CO? from the cooled compressed CO2 stream to form a condensed C<¾ stream. [0007 j Other embodiments, aspects, features, and advantages of the invention will become apparent to those of ordinary skill in the art from the foil owing detailed description, the accompanying drawings, and the appended claims.
BRIEF DESCRIPTION OF THE DRAWING FIGURES
10008| These and other features, aspects, and advantages of the present invention wiil become better understood when the following detailed description is read with reference to the accompanying drawings in which like characters represent like pails throughout the drawings, wherein: jO00 } FIG. 1 is a flow chart for a method of CO; condensation from a C<¾ stream, i accordance with one embodiment of the invention.
[00101 FIG. 2 is a flow chart for a melhod of C<¼ condensation from a C<¾ stream, i accordance with one embodiment of the invention.
[001 J j FIG. 3 is a biock diagram of a system for CO? condensation from a
CO?, stream, in accordance with one embodiment of the invention.
[0012 J FIG. 4 is a biock diagram of a system for CO?, condensation from a
C0j> stream, in accordance with one embodiment of the invention.
[0013| FIG. 5 is a biock diagram of a. system for CO? condensation from a
C<¼ stream, in accordance with one embodiment of the invention.
[0014! f'JG. 6 is a block diagram of a system for C02 condensation from a
CO;; stream, in accordance with one embodiment of the invention,
J0O153 PIG- 7 is a biock diagram of a system for C02 condensation from a
CO> stream, in accordance with one embodiment of the invention.
[0016J FIG. 8 is a block diagram of a system for CO? condensation from a
CO? stream, in accordance with one embodiment of the invention. [00 i 7 } FIG. 9 is a biock diagram of a system for CO? condensation from a
CO2 stream, in accordance with one embodiment of the invention. jOOlSj FIG. 10 is a pressure versus temperature diagram for CO2,
DETAILED DESCRIPTION
[0019} As discussed in detail below, embodiments of the present invention include methods and systems suitable for CO> condensation. As noted earlier, liquefying and pumping of CO2 may require high energy input. For example, a pressure o approximately 60 bar may be required to iiquefy CO2 at 20 °C. In some embodiments, an intermediate magnetic cooling step advantageously lowers the C{½ temperature to less than 0 *C, significantly reducing the required work of the overall system. In some embodiments, depending on the coefficient of performance of the magneto-caloric cooling system, an overall efficiency improvement of about 10 percent to about 15 percent may be possible using the methods and systems described herein.
[0020] Approximating language, as used herein throughout the specification and claims, may be applied to modify any quantitati e representation that could permissibly vary without resulting in a change in the basic function to which it is related. Accordingly, a value modified by a term or terms, such as "about", is not limited lo the precise value specified. In some instances, the approximating language may correspond to the precision of an. instrument for measuring the value.
J00213 i the following specification and the claims, the singular forms "a",
"an" and "the" include plural referenis unless the context clearly dictates otherwise. j ΟΟ223 i one embodiment, as shown in Figures ί and 3, a method 10 for condensing carbon dioxide from a CO2 stream i provided. The term "C02 stream", as used herein, refers to a stream of CO2 gas mixture emitted as a resul of the processing of fuels, such as. natural gas, bioroass. gasoline, diesel fuel coal, oil shale, fuel oil, tar sands, and combinations thereof, hi some embodiments, the€X¾ stream includes a C<¾ stream emitted from a gas turbine. In particular embodiments, the CO? stream includes a C<¾ gas mixture emitted from a coal or natural gas-fired power p!ani. j 0023 J In some embodiments, the CO? stream further includes one more of nitrogen, nitrogen dioxide, oxygen, or water vapor. In some embodiments, the CO2 stream further includes impurities or pollutants, examples of which include, but are not limited to, nitrogen, nitrogen oxides, sulfur oxides, carbon monoxide, hydrogen sulfide, un burnt hydrocarbons, particulate matter, and combinations thereof, in particular embodiments, the CO? stream is substantially free of the impurities or pollutants, in particular embodiments, the CO-> stream essentially includes carbon dioxide.
[002 j In some embodiments, the amount of impurities or pollutants in the
CO2 stream is less than about 50 mole percent, in some embodiments, the amount of impuriiies or polliitants in the CO: stream is less than about 20 mole percent. In some embodiments, the amount of impurities or pollutants in the CO? stream is in a range .from about 10 moie percent to about 20 mole percent. .In some embodiments, the amount of impurities or polliitants in the C02 stream is less than about 5 mole percent.
(0025) Irs one embodiment, the method includes receiving a CO2 stream 101 , as indicated in Fig. 3, from a hydrocarbon processing, combustion, gasification or a similar' power plant (not shown). As indicated in Figures 1 and 3, at step 1.1, the method 1.0 includes compressing and cooling the CO2 stream 101 t form a partiall cooled O2 stream 201. In some embodiments, the CO-> stream 301 may be compressed using or more compression stages 120. In some embodiments, the CO;j stream may be cooled using or more cooling stages 1.10.
|00261 In some embodiments, the CO stream 101 may be compressed to a desired pressure by using one or more compression stages, as indicated by 1 20 in Fig, 3. As indicated in Fig. 3, the compression stage 120 may further include one or more compressors, such as, 121 and 1 22, in some embodiments, it should be noted that in Fig. 3, the two compressors 1 25 and 1 22 are shown as an exemplars' embodiment only and the actual number of compressors and their individual configuration may vary depending on the end result desired. In one embodiment, the C > stream 101 may be conipressed to a pressure and temperature desired for the magnetic cooling and condensation steps 12 and 13, respectively. In some embodiments, the C<¾ stream 101 may be compressed to a pressure in a range from aboul 10 bar io about 60 bar prior to the magnetic cooling step 12. In particular embodiments, the CO? stream 101 may be compressed to a pressure in a range from about 20 bar to about 40 bar prior to the magnetic cooling step 12.
[0027 j In some embodiments, the COj stream 101 may be cooled to a desired temperature by using one or more cooling stages, as indicated by 1 10 in Fig. 3. As indicated in Fig, 3, the cooling stage 1 10 may further include one or more heat exchangers, such as, 1 i L 112 and 1 1 3, in some embodiments. II should be noted that in Fig. 3, the three heat exchangers 111 , 112, and 1 13 are shown as an exemplar? embodiment only and the actual number of heat exchangers id their individual configuration may vary depending on the end result desired. In some embodiments, one or more of the heat exchangers may be cooled using a cooling medium. In some embodiments, one more of the heat exchangers may be cooled using cooling air, cooling water, or both, as indicated by 1 15 in Fig. 3. In some embodiments, the cooling stage may further include one or more intereoolers to cool the exhaust gas stream 1 1 without affecting the pressure.
J0028] It should be further noted that in Fig. 3, the configuration of cooling stage 1 10 and compression stage 120 is shown as mi exemplary embodiment only and the actual configuration may vary depending on the end result desired. For example, in some other embodiments, the method may include cooling the CO2 stream in a heal exchanger 1 1 1 prior to compressing the CC¾ stream in a compressor 121. (not shown).
[0029] In some embodiments, the method further includes cooling the CO? stream 101 to a first temperature by expanding the CO¾ stream in one or more expanders 123, a indicated in Fig. 8. In some embodiments the method includes an expansion step that decreases the pressure of the CO? stream 10 i from absolute pressure levels greater than about 20 bar to pressure levels of around 20 bar, thereby decreasing ihe temperature of the C<¾ stream 101 to values iower than that may be reached by air or water cooling. Without being bound any theory, it is believed that by employing the expansion step, the overall duty of the magneto-caloric cooling step 12 may be reduced, as the inlet temperature of the partially -cooled CO? stream to the magneto-caloric step may be lower than thai without an expansion step. In some embodiments, the work extracted in the expansion step may be further used for the .magneto-caloric cooling step 12.
|0030j I one embodiment, the C<¾ stream .101 may be cooled to a temperature and pressure desired for the magnetic cooling and condensation steps 12 and 13. In one embodiment, the method includes compressing and cooling the CO?, stream 101 to form a partially cooled CO? stream 201, as indicated in Fig. 3. In one embodiment, the method further includes cooling the COj∑ stream 10 i to a first temperature by expanding the CO* stream in one or more expanders 123 to form the partially cooled C02. stream 201, as indicated in Fig. 8.
(0031 J In one embodiment, the method includes cooling the partially cooled
CO-2 stream 201 to a first temperature. In some embodiments, the partially cooled CO? stream 201 may be cooled to a temperature in a range from about 5 degrees Celsius lo about 35 degrees Celsius, prior to the magnetic cooling step 12. In particular embodiments, the partially cooled CO stream .201 may be cooled to a temperature in a range from about 10 degrees Celsius to about 25 degrees Celsius, prior to the magnetic cooling step 12.
[0032] As noted earlier, in the absence of an additional magnetic cooling step,
CO;; in the partially cooled C( stream 201 is typically liquefied at a temperature in a .range from about 20 degrees Celsius to about 25 degrees Celsi s. The condensation temperature is determined by the temperature of the cooling medium, which can be cooling water or air. As shown in Fig. 10, at a condensation temperature in a range from about 20 degrees Celsius to about 25 degrees Celsius, an absolute pressure of approximately 60 bar is required to liquefy CO?. In contrast, by cooling the CO? stream to a. temperature in a range from about -25 degrees Celsius to about 0 degrees Celsius, lower pressure may be advantageously used for condensing C<¾ from the partially cooled COi stream 201.
) 00331 in one embodiment, the .method further includes, at step 12, cooling the partially cooled CO2 stream 201 to a second temperature by magneto-caloric cooling to form a cooled CO2 stream 302. as indicated in Figures 1 and 3. In one embodiment, the method includes cooling the partiaily-cooled CO? stream 201 using a .magneto-caloric cooling stage 200, as indicated in Fig. 3,
(0034) In some embodiments, a magneto-caloric cooling stage 200 includes a heat exchanger 212 and an externa! magneto-caloric cooling device 21 1. In some embodiments, the magneto-caloric cooling device 21 1 is configured to provide coohng to the heat exchanger 212, as shown in Fig. 3.
[0035 J In one embodiment, the magneto-caloric cooling device 21 1 includes a cold and a hot heat exchanger, a permanent magnet assembly or an induction coil magnet assembly, a regenerator of magneto-caloric material, and a heat transfer fluid cycle. In one embodiment, the heat transfer fluid is pumped through the regenerator and the heal exchanger by a fluid pump (not shown).
(0036J In one embodiment, the magneto-caloric cooling devices works on an active magnetic regeneration cycle (AMR) and provides cooling power to a heat transfer fluid by sequential magnetization and demagnetization of the magneto-calorie regenerator with flow reversal heat transfer flow. In some embodiments, the sequential magnetizatio and demagnetization of the magneto-caloric regenerator may be provided for by a rotaiy set-up where the regenerator passes through a bore of the magnet system. In some other embodiments, the sequential magnetization and demagnetization of the magneto-caloric regenerator may be provided for by a reciprocating linear device. An exemplary magnet assembly and magneto-caloric cooling device are described in US Patent Application Serial No. 12/392J 15, filed on February 25, 2009, and incorporated herein by reference in. its entirety for any and all purposes, so long as not directly contradictor}' with the teachings herein. [0037 j In some embodiments, the heat at the hot heat exchanger may be delivered to the ambient environment In some other embodiments, the heal at the hot heat exchanger may be delivered to the return ilovv of the condensed and liquefied C<¾ after the pumping of the liquid C<¾, as described herein later.
[0038J As noted earlier, the magneto-caloric cooling stage further includes a heat exchanger 212. wherein the magneto-caloric cooling device 21 1 is configured to provide cooling to the heat exchanger 212. In one embodiment, the heat exchanger 212 is in fluid communication with the one or more cooling stages i 10 and the one or more compression stages 120. in one embodiment, the heat exchanger 212 is in fluid communication with the partially cooled Ci¾ stream 201 generated after the compression and cooling step 1 1 .
[0039} in some embodiments, the magneto-caloric cooling device 21 1 is configured to provide cooling to the heat exchanger 212 such thai the partially cooled C02. stream 2 1 is cooled to the second temperature. In one embodiment, the second temperature is in a range of from about 0 degrees Celsius to about-25 degrees Celsius. In one embodiment, the second temperature is in a range of from about 5 degrees Celsius to about-20 degrees Celsius. As noted earlier, the step 13 of cooling the partially-cooled CO;> stream in the magneto-caloric cooling stage results m a cooled C02 stream.
[0040} in some embodiments, the magneto-caloric cooling device 21 1 is configured to provide cooling to ihe heat exchanger 212 such that the partially cooled C02 stream 20 i is cooled to the second temperature, such that CO,; condenses from the cooled CO? stream. As noted earlier, the method includes compressing the CC stream 101 to a pressure in a range from about 20 bar to about 40 bar, in some embodiments. As indicated i Fig. 10, at a pressure level of 40 bar, the CC>> condenses at a temperature of 5 C. Further, as indicated in Fig. 10, at a pressure level of 20 bar. the Ct condenses at a temperature of -20 C.
[0041 j In one embodiment, the method further includes, at step 13. condensing at least a portion of C<¾. in the cooled CO2 stream at the second temperature, thereby condensing CO? from the cooled CO? stream to form a condensed CO? stream 302. In one embodiment, the method includes condensing at least portion of CO2 in the cooled CO2 stream at a pressure in a range of from about 20 bar to about 60 bar. In one embodiment, the method includes condensing at least a portion of CO2 in the cooled CO?, stream at a pressure in a range of from about 20 bar to about 40 bar. Accordingly, the method of the present invention advantageously allows for condensation of CO? at a lower pressure, in some embodiments.
[00421 In some embodiments, the method includes performing the steps of cooling the partially cooled CO? stream to form a cooled CO? stream Ϊ 2 and condensing CO2 from the cooled CO;? stream 13 simultaneously. In some other embodiments, the method includes performing the steps of cooling the partially cooled CO2 stream to form a cooled C<¾ stream 1 2 and condensing CO2 from the cooled CO2 stream 13 sequentially. j0043| As indicated in Fig. 3, in some embodiments, a cooled CO2 stream may be generated from the partially cooled O? stream 201 in the heat exchanger 212. In such embodiments, a portion of CO2 from the cooled CO? stream condenses in the heat-generator itself forming a condensed CO? stream 302, as indicated in Fig. 3.
[0044} In some other embodiments, as indicated in Fig. 4, a cooled CO?, stream 301 is generated from the partially cooled CO?, stream 201 in the heat exchanger 212. The method further includes transferring the cooled CO2 stream 3 1. to a condenser 213, as indicated in Fig. 4, in such embodiments, a portion of CO2 f om the cooied CO? stream 301 condenses in the condenser 213 and forms a condensed CO; stream 302, as indicated it) Fig. 4.
I 53 hi some embodiments, the method includes condensing at least about
95 weight percent of CO2 in the CO2 stream 101 to form the condensed CO2 stream 302, in some embodiments, the method includes condensing at least about 90 weight percent of CO2. in the Ct¼ stream 101 to form the condensed CO? stream 302. In some embodiments, the method includes condensing 50 weight percent to about 90 weight percent of CO? in the CO? stream 101 to form the condensed CO? stream 302. In some embodiments, the method includes condensing at least about 99 weight percent of CO? in the CO? stream 1 0.Ϊ to form the condensed CO? stream 302. j.00 6] In some embodiments, as noted earlier, the CO2 stream 101 further includes one or more components in addition to carbon dioxide. In some embodiments, the method further optionally includes generating a lean stream (indicated by doited arrow 202) after the steps of magneto-caloric cooling (step 12) and CO2 condensation (step 1.3). The term "lean stream" 202 refers to a siream in which the CO.; content is lower than that of the CO2 content in the CO.; stream. 101. In some embodiments, as noted earlier, almost all of the CO2 in the CO?, stream is condensed in the step 13. In such embodiments, the lean CO2 stream is substantially free of CO?, In some other embodiments, as noted earlier, a portion of the CO2 stream may not condense in the step 13 and the lean stream may include uncondensed CO2 gas mixture,
[0 473 In some embodiments, the lean stream 202 may include one or more non-condensable components, which may not condense i the step 13. In some embodiments, the lean stream 202 may include one or more liquid components. In such embodiments, the lean stream may be further configured to be in fluid communication with a liquid-gas separator. In some embodiments, the lean stream 202 may include one or more of nitrogen, oxygen, or sulfur dioxide.
[0048} In some embodiments, the method may further include dehumidilying the CO2 stream 101 before step 1 1. In some embodiments, the method may further include dehumidtfying the partially cooled CO? stream 201 after step I I and before step 1 2. In some embodiments, the system 1 00 may further include a dehumidifier configured to be in flow communication (not. shown) with the CO? siream 101. In some embodiments, the system 100 may further include a dehumidifier configured to be in flow communication {not shown) with the CO3 stream 101.
[004 j In some embodiments, the method further includes circulating the condensed CO2 stream 302 to one or more cooling stages used for cooling the CO? stream. As indicated in Fig, 5, the method further includes Circulating the condensed CO2 stream to a heal exchanger 1 13 via a circulation loop 303. In such embodiments, the method further includes a recuperation step where the condensed COj stream is circulated back to further cool the partially cooled CO? stream 201 before the magnet o-caioric cooling step 12, in some embodiments, the recuperation step may increase the efficiency of the magneto-caloric step.
(00501 to some embodiments, the recuperation of condensed CO?, stream to the heat exchanger 113 may result in cooling of the partially cooled CO2 stream 201 below the temperature required for condensation of CO2. In some embodiments, the method may further include condensing the CO?, in the partially cooled CO? stream 20.1 to form a recuperated condensed CO2 stream 501 , as indicated in Fig. 5.
[0051 j In some embodiments, the method .further includes increasing a pressure of the condensed C O.. stream 302 using a pump 300. as indicated in Fig, 3. In embodiments including a recuperation step, the method may further include increasing a pressure of the recuperated condensed CO2 stream 50.1 using a pump 300. as indicated in Fig. 5. In some embodiments, the method includes increasing a pressure of the condensed C<¼ stream 302 or the recuperated condensed CO2 stream 502 to a pressure desired for CO2 sequestration or end -use. In some embodiments, the method includes increasing pressure of the condensed CO2 stream 302 or the recuperated condensed CO2 stream 502 to a pressure in a range from about 150 bar to about 180 bar,
J00521 in some embodiments, the method further includes generating a pressurized CO?, stream 401 after the pumping step. In some embodiments, the method further includes generating a supercritical CO? stream 401 after the pumping step. In some embodiments, as noted earlier, the pressurized CO stream 401 may be used for enhanced oil recovery, CO storage, or CO2 sequestration.
[0053} In some embodiments, a system 100 for condensing carbon, dioxide
(CO?) from a CO2 stream 1 1 is provided, as illustrated in Figures 3-9. In one embodiment, the system 100 includes one or more compression stages 120 configured
1:2 to receive the C(¾ stream 1 01 . The system i 00 further includes one or more cooling stages 1 10 in fluid communication with the one or more compression stages 120. In one embodiment a combination of the one or more compression stages .120 and the one or more cooling stages 1 1 is configured to compress and cool the CO2 stream 101 to a first temperature lo form a partially-cooled CO?; stream 201.
J 0054} in one embodiment, the system 100 further includes a magneto-caloric cooling stage 200 configured to receive the partially-cooled€(¾, stream 201 and coo! the partially-cooled CO2 stream 201 to a second temperature to form a cooled CO> stream 301. As noted earlier, the magneto-caloric cooling stage 200 further includes a heat exchanger 212, wherein the magneto-caloric cooling device 21 1 is configured to provide cooling to the heat exchanger 212. In one embodiment, the heat exchanger 21 2 is in fluid communication with the one or more cooling stages 1 1 and the one or more compression stages 120. j 055j As noted earlier, in some embodiments, the heat exchanger 212 is configured to condense a portion of CO2 in the partially cooled CO2 stream 201 to form the condensed CO2 stream 302. In some oilier embodiments, the system 100 further includes a condensation stage 213 configured to condense a portion of C<¼ in the cooled CO2 stream 301 at the second temperature, thereby condensing CO2 from the cooled CO2 stream 301 to form a condensed CO2 stream 302.
[0056j In some embodiments, the system 100 further includes a pump 300 configured io recei ve the condensed CO2 stream 302 and increase the pressure of the condensed CO2 stream 302. In some embodiments, the system further includes a circulation loop 303 configured to circulate a portio of the condensed C<¾ stream 302 to the one or more cooling stages 1 10.
I 573 With the foregoing in mind, systems and methods for condensing CO2 from a CO? stream, according lo some exemplary embodiments of the invention, are further described herein. Turning now to Figures 2 and 3, in one embodiment, a meihod 20 of condensing carbon dioxide from a CO2 stream 1 01 is provided. In one embodiment, the method includes, at step 21 , cooling the CO stream 101 in a first cooling stage including a first heat exchanger 111 to form a first partially cooled CO? stream 102. n one embodiment, the method includes, at step .2.2. compressing the ■first partially cooled C02 stream 102 in a first compressor 1 21 to form a first compressed CO? stream 103. In one embodiment, the method includes, at step 23, cooling the first compressed CO;? stream 103 in a second cooling stage including a second heat exchanger 1 1.2 to form a second partially cooled COi stream 104. In one embodiment, the method includes, at step 24, compressing the second partially cooled CO? stream "104 in a second compressor 122 to form a second compressed CO; stream 105. In one embodiment, the method includes, at step 25, cooling the second compressed CO? stream 105 to a first temperature in a third cooling stage comprising a third heat exchanger 1 1.3 to form a partiall cooled COj> stream 2 1.
}00S8j in one embodiment, the method 20 includes, at step 26, cooling the partially cooled CO.; stream 201 to a second temperature fay magneto-caloric cooling using a magneto-caloric cooling stage 200 to form a cooled CO? stream (not shown). In some embodiments, a magneto-caloric cooling stage .200 includes a heat exchanger 212 and an external magneto-caloric cooling device 21.1. In some embodiments, the magneto-caloric cooling device 211 is configured to provide cooling to the heat exchanger 212. as indicated in Fig, 3.
[0059 j In one embodiment, the method includes, at step 27, condensing at least a portion of CO? in the cooled CO siream at the second temperature, thereby condensing C<¾ from the cooled CO? stream to form a condensed C<¾ stream 302. As noted earlier, in some embodiments, a cooled CO? stream is generated from the partially cooled CO? stream 20.1 in the heal exchanger 212. In such embodiments, a portion of CO2 from the cooled CO? stream condenses in the heat-generator itself .forming a condensed C<¾ stream 302, as indicated in fig. 3.
(0060 j In some embodiments, the method further includes increasing a pressure of the condensed CO? stream 302 using a pump 300, as indicated in Fig. 3. In some embodiments, the method further includes generating a pressurized CO , stream 401 after the pumping step, in some embodiments, as noted earlier, the pressurized CC stream 401 may be used for enhanced oil recovery-, CO? storage, or C02 sequestration.
[0061 j Turning no to Fig. 4, in one embodiment, a method and a system for condensing CO2 from a CO2 stream 101 is provided. The method and system is similar to the system and method illustrated in Fig. 3. with the addition that the method further includes transferring the cooled CO;j stream 301 to a condenser 213, as indicated in Fig. 4. In such embodiments, a portion of CO; from the cooled CO2 stream 301 condenses in the condenser 213 and forms a condensed C<¾ stream 302, as indicated in Fig. 4.
[0062] Turning now to Fig. 5, in one embodiment, a method and system for condensing CO;? from a CO? stream 101 is provided. The method and system is similar to the system and method illustrated in Fig. 3. with the addition that the method further includes circulating a portion of the condensed CO2 stream 302 to the third heat exchanger 113 via a circulation loop 303. As noted earlier, in some embodiments, the recuperation of condensed CO2 stream to the heat exchanger 1 13 may result in cooling of the second compressed CO2 stream 105 below the temperature required for condensation of CO^. In some embodiments, the method may further include condensing the CO2 in the second compressed CO;? stream 105 to form a recuperated condensed CO2 stream 501 , as indicated in Fig. 5.
[0063 J Turning now to Fig. 6. i one embodiment, a method and s stem for condensing O> from a CO2 stream 101 is provided. The method and system is similar to the system and method illustrated in Fig. 4. with the addition that the method further includes circulating a portion of the condensed CO? stream to the third heat exchanger 113 via a circulation loop 303. As noted earlier, in some embodiments, the recuperation of condensed CO2 to the heat exchanger 113 may result in cooling of the second compressed CO2 stream 105 helow the temperature required for condensation of CO?, in some embodiments, the method may further include condensing the COj in the second compressed CO3 stream 105 to form a recuperated condensed CO2 stream 501. as indicated in Fig. 6. [0064 j Turning now to Fig. 7, in one embodiment a method mid a system for condensing CO? from a CO2 stream 101 is provided. The method and system is similar to (he system and method illustrated in Fig. 3. with the addition that the method further includes circulating a portion, of the pressurized C<¾ stream 401 to the third heat exchanger 113 via a circulation !oop 403. As noted earlier, in some embodiments, the recuperaiion of pressurized C<¾. stream 401 to the third heat exchanger 1 1.3 .may result in cooling of the second compressed C02 stream 1.05 below the temperature required for condensation of CO?, in some embodiments, the method may further include condensing the CO?, in the second compressed CO?, stream 105 to form a recuperated condensed CO2 stream 501 , as indicated in Fig. 7. j 00651 Turning now to Fig. 8, in one embodiment, a method id a system for condensing CO? from a 2 stream 101 is illustrated. The method and system is similar to the system and method illustrated i Fig. 3, with the addition that the method further includes forming a third partially cooled CO2 stream 106 in the third heat exchanger 1 . 3. The method further includes cooling the third partially cooled CO : stream 106 to a first temperature by expanding the third partially cooled CO? stream 106 in one or more expanders 123, before the magneto-caloric cooling step, to form the parti all -cooled CO?, stream 201 , as indicated i Fig. 8.
[0066] Turning now to Fig. 9, in one embodiment, a method and a system for condensing CO2 from a CO? stream 101 is illustrated. The method and system is similar to the system and method illustrated in Fig. 8, with the addition that the third cooling stage further comprises a fourth beat exchanger 114, and the method further includes circulating a portion of the pressurized CO2 stream 401 to the fourth heat exchanger 1 14 via a circulation loop 403. The .method further includes forming a fourth partially cooled C<¾ stream 107 after the expansion step and transferring the fourth partially cooled CO2 stream 107 to the fourth heat exchanger 1 14. As noted earlier, in some embodiments, the recuperation of pressurized C<¾. stream 401 to the fourth heat exchanger 1 14 may result in cooling of the fourth partially cooled C02 stream 107 below the temperature required for condensation of CO?, In some embodiments, the method may further include condensing the C<¼ in the fourth partially cooled CO.: stream 107 io form a recuperated condensed COj> stream 501, as 'indicated in Fig. 9.
[0067} As noted earlier, some embodiments of the invention advantageously allo for cooling of the supercritical CCh to lower temperatures and subsequent condensation at lower pressures than those available through conventional cooling methods, such as, vapor compression. Without being 'bound by any theory, it is believed thai compression of supercritical COj may he less efficient than pumping liquid CCh- Thus, in some embodiments, the method reduces the penalty on the less- efficient COj compression step, in some embodiments, the method may reduce the overall penalty for C< . liquefaction and pumping by improving the efficiency of the compression and pumping system. In some embodiments, the magneto-caloric cooling stage may reduce the penalty by more than 10%. In some embodiments, the magneto-caloric cooling stage may reduce the penalty fay more than 20%. In some embodiments, the overall plant efficiency may be improved by using one or more of the method embodiments, described herein,
[0068] Further, some embodiments of the invention advantageously allow for improved range of operabilify of CCb compression and liquefaction systems. In conventional CO;> compression mid iiquefaction systems, the ambient temperature of the cooling air or cooling water may limit the range of operabiiity. Supercritical CO2 may not liquefy at temperatures greater than about 32 °C, the critical temperature of CO2. Thus, when ambient temperatures are above 30 ° , liquefaction of C<¾ may be difficult without additional external cooling, in some embodiments, the magnetic cooling step may advantageously allow cooling of CO.; to the sufacriticaS range, thereby enabling the operabiiity of the compression and liquefaction systems under any ambient conditions.
[0069| This written description uses examples to disclose the invention, including the best mode, and also to enable any person skilled in the art to practice the invention, including making and using any devices or systems and performing any incorporated methods. The patentable scope of the invention is defined by the claims, and may include other examples that occur to those skilled in the art. Such other examples are intended to be within ihe scope of the claims if ihe have structural elements that do nol differ from the literal language of the claims, or if they include equivalent structural elements with insubstantial differences from the literal language of the claims.

Claims

What is claimed is:
1. A method of condensing carbon dioxide (CO2) from a CO?, stream, comprising:
(i) compressing and cooling the CO2 stream to form a partially cooled CO? stream, wherein the partially cooled CO> stream is cooled to a first temperature
(u) cooling the partially cooled CO? stream to a second temperature by magnet o-caioric cooling to form a cooled CO stream; and
(iii) condensing ai least a portion of CO> in the cooled CO2 stream to form a condensed CO; stream.
2. The method of claim i , wherein step (iii) comprises condensing at least a portion of CO? in ihe cooled CO? stream at a pressure in a range of from about 20 bar to about 60 bar.
3. The method of claim i , wherein step (iii) comprises condensing at least a portion of CO? in the cooled CO? stream at a pressure in a range of from about 20 bar to about 40 bar.
4. The method of claim 1, wherein the first temperature is in a range of from about 5 degrees Celsius to about 35 degrees Celsius
5. The method of claim 1 , wherein the second temperature is in a range of from about 0 degrees Celsius to about-25 degrees Celsius
6. The method of claim 1 , wherein step (i) comprises cooling the€(¾ stream using one or .more cooling stages comprising one or more heal exchangers.
7. The method of claim 5 , further comprising circulating a portion of the condensed CO? stream to one or more cooling stages used for cooling the C(¾ stream,
8. The method of claim 1 , wherein step (i) comprises cooling the C(¾ stream to the first temperature by expanding the CO2 stream in one or more expanders.
9. The method of claim 1 , wherein step (ii) comprises cooling the partially- cooled C<¾. stream using a rotary magneto-caloric cooling device.
10. The method of claim 1, further comprising increasing a pressure of the condensed Ctb stream using a pump to form a pressurized CC , stream.
1 1 . A method of condensing carbon dioxide (CO ) from a CO stream, comprising:
(i) cooling the CO - stream in a first cooling stage comprising a first heat exchanger to form a first partially cooled CO2 stream;
(ii) compressing the first partially cooled €<¾ stream to form a first compressed CO2 stream;
(iii) cooling the first compressed CO; stream i a second cooling stage comprising a second heat exchanger to form a second partially cooled CO> stream; (iv) compressing the second partially cooled C(¾ stream to form a second compressed COi stream;
(v) cooling the second compressed CO?, stream to a first temperature in a third cooling stage comprising a third heat exchanger t form a partially cooled C(¾ stream;
(vi) cooling the partially cooled CO? stream to a second temperature by magneio-calonc cooling 10 form a cooled CO?, stream; and i ii ) condensing at least a portion of CO in the cooled CO? stream at the second temperature, thereby condensing CO? from the cooled CO?, stream to form condensed CO? stream.
12. The method of claim ί L further comprising circulating a portion of the condensed CO? stream to the third heat exchanger.
13. The method of claim 1 i , wherein the third cooling stage further comprises an expander, and step (v) further comprises cooling the CO2 stream to a first temperature by expanding the second compressed COj stream in the expander,
14. The method of claim 13, wherein the third cooling stage further comprises a fourth heat exchanger, and the method further comprises circulating a portion of the condensed CO? stream to the fourth heat exchanger.
15. A system for condensing carbon dioxide (CO?) from a CO? stream, comprising;
(i ) one or .more compression stages configured to recei e the CO? stream;
2. (ii) one or more cooling stages in fluid communication wiih the one or more compression stages, wherein a combination of the one or more compression stages and the one or more cooling stages is configured to compress and cool the CO2 stream to a first temperature io form a partially-cooled CO? stream;
(Hi) a magento-caloric cooling stage configured io receive the partially-cooled CO2 stream and cooi the partially-cooled CO? stream io a second temperature to form a cooled (X>2 stream.; and
(iv) a condensation stage configured to condense a portion of CO?, in the cooled C0j> stream ai the second temperature, thereby condensing CO? from the cooled CO? stream to form a condensed CO? stream.
16. The system of ciaim 1 . wherein the magneto-caloric cooling stage comprises a magneto-caloric cooling device and a heat exchanger, wherei the heat exchanger is in fluid communication with the one or more cooling stages and the one or more compression stages.
. 7, The system of claim 15, further comprising a pump configured to receive the condensed CO.; stream and increase the pressure of the condensed C02 stream.
18. The system of claim 15, wherein the one or more cooling stages further comprises an expander.
19. The system of claim 15, wherein the one or more cooling stages comprises one or more heal exchangers configured to coo! the CO> stream using air, water, or combinations thereof.
20. The system of claim 15, further comprising a circulation loop configured to circulate a portion of the condensed CO? stream to the one or more cooling stages.
EP12775386.1A 2011-09-30 2012-09-28 Methods and systems for co2 condensation Pending EP2815194A2 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US13/249,464 US20130081409A1 (en) 2011-09-30 2011-09-30 Methods and systems for co2 condensation
PCT/US2012/057860 WO2013049532A2 (en) 2011-09-30 2012-09-28 Methods and systems for co2 condensation

Publications (1)

Publication Number Publication Date
EP2815194A2 true EP2815194A2 (en) 2014-12-24

Family

ID=47046861

Family Applications (1)

Application Number Title Priority Date Filing Date
EP12775386.1A Pending EP2815194A2 (en) 2011-09-30 2012-09-28 Methods and systems for co2 condensation

Country Status (11)

Country Link
US (1) US20130081409A1 (en)
EP (1) EP2815194A2 (en)
JP (1) JP6154813B2 (en)
KR (1) KR101983343B1 (en)
CN (1) CN104471335B (en)
AU (1) AU2012315807C1 (en)
BR (1) BR112014005676B1 (en)
CA (1) CA2848991C (en)
MX (1) MX2014003880A (en)
RU (1) RU2606725C2 (en)
WO (1) WO2013049532A2 (en)

Families Citing this family (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BR112017012856A2 (en) * 2014-12-18 2018-01-09 Basf Se magnetocaloric cascade, magnetocaloric regenerator, heat pump, method for manufacturing a magnetocaloric cascade, heat pumping method
FR3033397A1 (en) * 2015-03-06 2016-09-09 Air Liquide PROCESS FOR COMPRESSING AND COOLING A GASEOUS MIXTURE
CA3075639A1 (en) * 2017-09-19 2019-03-28 Honeywell International Inc. Heat transfer methods, systems and compositions
CN109813054B (en) 2017-11-22 2021-03-30 斗山重工业建设有限公司 Carbon dioxide capture device using cold energy of liquefied natural gas and power generation system
IT201800009221A1 (en) * 2018-10-05 2020-04-05 Graf Spa SERVICE STATION FOR MEANS OF TRANSPORT
US11224837B2 (en) * 2018-11-12 2022-01-18 Linde Aktiengesellschaft Post-combustion carbon dioxide capture and compression
CN112678825A (en) * 2020-12-31 2021-04-20 起时超临界高新技术(广州)有限公司 Built-in heat exchange type supercritical carbon dioxide separation method and equipment
US11635255B1 (en) * 2022-04-08 2023-04-25 Axip Energy Services, Lp Liquid or supercritical carbon dioxide capture from exhaust gas
FR3137164A1 (en) * 2022-06-24 2023-12-29 IFP Energies Nouvelles Carbon dioxide compression system and method with multiphase compression and supercritical pump

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6588215B1 (en) * 2002-04-19 2003-07-08 International Business Machines Corporation Apparatus and methods for performing switching in magnetic refrigeration systems using inductively coupled thermoelectric switches
US20080236171A1 (en) * 2006-09-28 2008-10-02 Kabushiki Kaisha Toshiba Magnetic refrigerating device and magnetic refrigerating method
WO2008122535A1 (en) * 2007-04-05 2008-10-16 Universite Henri Poincare Nancy 1 New intermetallic compounds, their use and a process for preparing the same
EP2196251A1 (en) * 2008-12-04 2010-06-16 Siemens Aktiengesellschaft Carbon dioxide separation device and method of operating such a device

Family Cites Families (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1780250A (en) * 1930-03-27 1930-11-04 Frank G Campbell Method of and apparatus for liquefying gases
JPS576283A (en) * 1980-06-12 1982-01-13 Nippon Oxygen Co Ltd Carbon dioxide removal of air separator
US5893275A (en) * 1997-09-04 1999-04-13 In-X Corporation Compact small volume liquid oxygen production system
US5927103A (en) * 1998-06-17 1999-07-27 Praxair Technology, Inc. Carbon dioxide production system with integral vent gas condenser
US6035662A (en) * 1998-10-13 2000-03-14 Praxair Technology, Inc. Method and apparatus for enhancing carbon dioxide recovery
US6210467B1 (en) * 1999-05-07 2001-04-03 Praxair Technology, Inc. Carbon dioxide cleaning system with improved recovery
RU2175949C2 (en) * 1999-07-27 2001-11-20 ЗАО "Центр ВМ-Технологий" Method of cleaning carbon dioxide from low-boiling impurities
JP2003532861A (en) * 2000-05-05 2003-11-05 ユニヴァーシティ オブ ヴィクトリア イノヴェーション アンド デヴェロップメント コーポレイション Apparatus and method for cooling and liquefying a fluid using magnetic refrigeration
US6293106B1 (en) * 2000-05-18 2001-09-25 Praxair Technology, Inc. Magnetic refrigeration system with multicomponent refrigerant fluid forecooling
GB2416389B (en) * 2004-07-16 2007-01-10 Statoil Asa LCD liquefaction process
EP1736719A1 (en) * 2005-06-20 2006-12-27 Haute Ecole d'Ingénieurs et de Gestion du Canton Continuously rotary magnetic refrigerator or heat pump
US8555672B2 (en) * 2009-10-22 2013-10-15 Battelle Energy Alliance, Llc Complete liquefaction methods and apparatus
US8209988B2 (en) * 2008-09-24 2012-07-03 Husssmann Corporation Magnetic refrigeration device
US8617292B2 (en) * 2009-12-15 2013-12-31 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Method of obtaining carbon dioxide from carbon dioxide-containing gas mixture
US20120174621A1 (en) * 2011-01-06 2012-07-12 General Electric Company Carbon dioxide liquefaction system
DE112011104855T5 (en) * 2011-02-08 2013-11-07 Ihi Corporation Exhaust gas treatment system for oxy-fuel combustion device

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6588215B1 (en) * 2002-04-19 2003-07-08 International Business Machines Corporation Apparatus and methods for performing switching in magnetic refrigeration systems using inductively coupled thermoelectric switches
US20080236171A1 (en) * 2006-09-28 2008-10-02 Kabushiki Kaisha Toshiba Magnetic refrigerating device and magnetic refrigerating method
WO2008122535A1 (en) * 2007-04-05 2008-10-16 Universite Henri Poincare Nancy 1 New intermetallic compounds, their use and a process for preparing the same
EP2196251A1 (en) * 2008-12-04 2010-06-16 Siemens Aktiengesellschaft Carbon dioxide separation device and method of operating such a device

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of WO2013049532A2 *

Also Published As

Publication number Publication date
BR112014005676B1 (en) 2021-07-20
AU2012315807B2 (en) 2017-06-22
MX2014003880A (en) 2014-05-07
US20130081409A1 (en) 2013-04-04
WO2013049532A3 (en) 2015-01-29
JP2015507731A (en) 2015-03-12
AU2012315807A1 (en) 2014-04-10
WO2013049532A2 (en) 2013-04-04
CA2848991C (en) 2020-07-21
CN104471335B (en) 2017-11-07
JP6154813B2 (en) 2017-06-28
RU2014110121A (en) 2015-11-10
RU2606725C2 (en) 2017-01-10
KR20140089527A (en) 2014-07-15
CA2848991A1 (en) 2013-04-04
CN104471335A (en) 2015-03-25
KR101983343B1 (en) 2019-05-28
AU2012315807C1 (en) 2017-11-16
BR112014005676A2 (en) 2017-04-04

Similar Documents

Publication Publication Date Title
AU2012315807C1 (en) Methods and systems for co2 condensation
US20130025294A1 (en) System and method for carbon dioxide removal
US20020148225A1 (en) Energy conversion system
AU2015315557B2 (en) Production of low pressure liquid carbon dioxide from a power production system and method
US9766011B2 (en) Optimized heat exchange in a CO2 de-sublimation process
KR20140043745A (en) Process for liquefaction of natural gas
EA016746B1 (en) Method and system for production of liquid natural gas
MX2012014459A (en) Stoichiometric combustion with exhaust gas recirculation and direct contact cooler.
CA2805336C (en) Energy efficient production of co2 using single stage expansion and pumps for elevated evaporation
Pei et al. Waste heat recovery in CO2 compression
AU2011222674B2 (en) Method and installation for liquefying flue gas from combustion installations
Moore et al. Novel concepts for the compression of large volumes of carbon dioxide
EP2508721B1 (en) Integrated gasification combined cycle system with vapor absorption chilling
EP2596846A1 (en) Expander and method for CO2 separation
KR101082349B1 (en) Carbon Dioxide Liquefaction Equipment Using Internal Heat Exchange
Carpenter Process Reduces Carbon Emissions From Natural Gas Compression and Production
CN102853633B (en) Air-separating plant and include the system of this air-separating plant
BOLLAND et al. NATURAL GAS FIRED POWER CYCLES WITH INTEGRATED CO: CAPTURE', HENRIETTE UNDRUM2 AND MICHEL V1YHRE h

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20140402

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

DAX Request for extension of the european patent (deleted)
R17D Deferred search report published (corrected)

Effective date: 20150129

R17P Request for examination filed (corrected)

Effective date: 20150729

RBV Designated contracting states (corrected)

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

17Q First examination report despatched

Effective date: 20161004

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

P01 Opt-out of the competence of the unified patent court (upc) registered

Effective date: 20230526