EP2815194A2

EP2815194A2 - Methods and systems for co2 condensation

Info

Publication number: EP2815194A2
Application number: EP12775386.1A
Authority: EP
Inventors: Miguel Angel Gonzalez Salazar; Vittorio Michelassi; Christian Vogel
Original assignee: General Electric Co
Current assignee: General Electric Co
Priority date: 2011-09-30
Filing date: 2012-09-28
Publication date: 2014-12-24
Also published as: MX376497B; JP2015507731A; BR112014005676B1; JP6154813B2; US20130081409A1; MX2014003880A; KR20140089527A; CN104471335A; CA2848991C; RU2014110121A; AU2012315807B2; AU2012315807A1; WO2013049532A3; AU2012315807C1; CA2848991A1; RU2606725C2; WO2013049532A2; CN104471335B; BR112014005676A2; KR101983343B1

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 CO₂stream. 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 recover^y-, 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.