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.
• 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.

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