Purification of carbon dioxide

• US 10,254,042 B2
• Filed: 10/25/2013
• Issued: 04/09/2019
• Est. Priority Date: 10/25/2013
• Status: Active Grant

• Current Assignee: Air Products and Chemicals Incorporated (Linde Plc)
• Original Assignee: Air Products and Chemicals Incorporated (Linde Plc)
• Inventors: Higginbotham, Paul, Guvelioglu, Galip Hakan, Palamara, John Eugene, White, Vincent
• Primary Examiner(s): Alosh, Tareq
• Application Number:
  US14/063,047
• Publication Number:
  US 20150114033A1
• Time in Patent Office: 1,992 Days
• CPC Class Codes: B01D 2257/302 Sulfur oxides
• CPC Class Codes: B01D 2257/304 Hydrogen sulfide
• CPC Class Codes: B01D 2257/306 Organic sulfur compounds, e.g. mercaptans
• CPC Class Codes: B01D 2257/308 Carbonoxysulfide COS
• CPC Class Codes: B01D 2257/404 Nitrogen oxides other than dinitrogen oxide
• CPC Class Codes: B01D 2257/406 Ammonia
• CPC Class Codes: B01D 2257/7022 Aliphatic hydrocarbons
• CPC Class Codes: B01D 53/002 by condensation
• CPC Class Codes: B01D 53/75 Multi-step processes
• CPC Class Codes: C01B 17/167 Separation
• CPC Class Codes: C01B 32/50 Carbon dioxide
• CPC Class Codes: F25J 2200/04 in a dual pressure main column system
• CPC Class Codes: F25J 2200/08 in a triple pressure main column system
• CPC Class Codes: F25J 2200/10 in a quadruple, or more, column or pressure system
• CPC Class Codes: F25J 2200/40 Features relating to the provision of boil-up in the bottom of a column
• CPC Class Codes: F25J 2200/50 using multiple (re-)boiler-condensers at different heights of the column
• CPC Class Codes: F25J 2200/70 Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
• CPC Class Codes: F25J 2200/74 Refluxing the column with at least a part of the partially condensed overhead gas
• CPC Class Codes: F25J 2200/76 Refluxing the column with condensed overhead gas being cycled in a quasi-closed loop refrigeration cycle
• CPC Class Codes: F25J 2200/78 Refluxing the column with a liquid stream originating from an upstream or downstream fractionator column
• CPC Class Codes: F25J 2205/02 : using simple phase separation in a vessel or drum
• CPC Class Codes: F25J 2205/30 : using a washing, e.g. "scrubbing" or bubble column for purification purposes
• CPC Class Codes: F25J 2205/40 : using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
• CPC Class Codes: F25J 2205/80 : using membrane, i.e. including a permeation step
• CPC Class Codes: F25J 2215/80 : Carbon dioxide
• CPC Class Codes: F25J 2220/82 : Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
• CPC Class Codes: F25J 2220/84 : Separating high boiling, i.e. less volatile components, e.g. NOx, SOx, H2S
• CPC Class Codes: F25J 2230/80 : the fluid being carbon dioxide
• CPC Class Codes: F25J 2235/02 : using a pump in general or hydrostatic pressure increase
• CPC Class Codes: F25J 2235/80 : the fluid being carbon dioxide
• CPC Class Codes: F25J 2240/40 : Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
• CPC Class Codes: F25J 2245/02 : Recycle of a stream in general, e.g. a by-pass stream
• CPC Class Codes: F25J 2260/20 : Integration in an installation for liquefying or solidifying a fluid stream
• CPC Class Codes: F25J 2260/80 : Integration in an installation using carbon dioxide, e.g. for EOR, sequestration, refrigeration etc.
• CPC Class Codes: F25J 2270/02 : Internal refrigeration with liquid vaporising loop
• CPC Class Codes: F25J 2270/80 : Quasi-closed internal or closed external carbon dioxide refrigeration cycle
• CPC Class Codes: F25J 2270/88 : Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided
• CPC Class Codes: F25J 2290/40 : Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.
• CPC Class Codes: F25J 3/0257 : separation of nitrogen from air F25J3/04, production of nitrogen in general C01B21/00
• CPC Class Codes: F25J 3/0266 : separation of carbon dioxide production of carbon dioxide in general C01B32/00
• CPC Class Codes: F25J 3/029 : of helium
• CPC Class Codes: F25J 3/08 : Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixturescold traps B01D8/00
• CPC Class Codes: Y02B 30/52 : Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency
• CPC Class Codes: Y02C 20/40 : of CO2
• CPC Class Codes: Y02P 20/10 : Process efficiency
• CPC Class Codes: Y02P 20/129 : Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
• CPC Class Codes: Y02P 20/151 : Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Abstract

In a process for separating at least one “heavy” impurity such as hydrogen sulfide from crude carbon dioxide comprising significant quantities of at least one “light” impurity such as non-condensable gases, involving at least one heat pump cycle using carbon dioxide-containing fluid from the process as the working fluid, the “light” impurity is removed from the crude carbon dioxide and carbon dioxide is subsequently recovered from the removed “light” impurity, thereby improving overall carbon dioxide recovery and efficiency in terms of energy consumption.

Claims

1. A process for purifying crude carbon dioxide fluid comprising at least one “

light”

impurity and at least one “

heavy”

impurity, said process comprising;

cooling said crude carbon dioxide fluid above the triple point pressure of carbon dioxide by indirect heat exchange to produce a cooled crude carbon dioxide fluid;

feeding said cooled crude carbon dioxide fluid to a first column system for mass transfer separation to produce a “

light”

impurity-enriched overhead vapor and a “

light”

impurity-depleted carbon dioxide bottoms liquid comprising said “

heavy”

impurity;

re-boiling said first column system by vaporizing a portion of said “

light”

impurity-depleted carbon dioxide bottoms liquid by indirect heat exchange to provide a vapor for said first column system;

feeding a further portion of said “

light”

impurity-depleted carbon dioxide bottoms liquid from said first column system to a second column system for mass transfer separation to produce a carbon dioxide-enriched overhead vapor and a “

heavy”

impurity-enriched bottoms liquid;

providing a carbon dioxide-enriched liquid as reflux for said second column system;

re-boiling said second column system by indirect heat exchange to provide a vapor for said second column system;

wherein said first and second column systems operate above the triple point pressure and below the critical pressure of carbon dioxide;

wherein said process comprises at least one heat pump cycle using as working fluid a portion of said carbon dioxide-enriched overhead vapor from said second column system;

wherein said second column system is re-boiled by at least partially vaporizing a portion of said “

heavy”

impurity-enriched liquid in or taken from said second column system by indirect heat exchange against said working fluid of said at least one heat pump cycle;

wherein said overhead vapor from said first column system comprises carbon dioxide and at least a portion of said carbon dioxide is recovered from said overhead vapor from said first column system to produce a “

light”

impurity-rich residual gas and a recovered carbon dioxide; and

wherein said recovered carbon dioxide is fed to said second column system for mass transfer separation.

2. The process of claim 1, wherein said cooled crude carbon dioxide fluid is expanded prior to being fed to said first column system.

3. The process of claim 2, wherein said cooled crude carbon dioxide fluid is below the critical pressure of carbon dioxide prior to expansion.

4. The process of claim 1, wherein said overhead vapor from said first column system is cooled prior to said carbon dioxide recovery.

5. The process of claim 4, wherein said cooling of said overhead vapor from said first column system is by indirect heat exchange to condense carbon dioxide in the overhead vapor from said first column system which is recovered by phase separation.

6. The process of claim 1, wherein said second column system comprises at least two distillation sections and said further portion of said “

light”

impurity depleted carbon dioxide bottoms liquid from said first column system is fed to said second column system at an intermediate zone between adjacent distillation sections.

7. The process of claim 6, wherein said second column system is additionally re-boiled by vaporizing a liquid in or taken from said or another intermediate zone.

8. The process of claim 1, wherein said crude carbon dioxide fluid is either a vapor that is at least partially condensed during said cooling, or a supercritical fluid that is “

pseudo-condensed”

during said cooling, to produce said cooled crude carbon dioxide fluid.

9. The process of claim 8, wherein said cooled crude carbon dioxide fluid is expanded prior to being fed to said first column system.

10. The process of claim 8, wherein re-boil duty for said first column system is provided at least in part by indirect heat exchange against condensing, or pseudo-condensing, said crude carbon dioxide fluid.

11. The process of claim 1, wherein said first column system comprises a distillation column system, said cooled crude carbon dioxide fluid being fed to said distillation column system for distillation to produce said “

light”

impurity-enriched overhead vapor and said “

light”

impurity-depleted carbon dioxide bottoms liquid.

12. The process of claim 1, wherein said at least one “

light”

impurity comprises at least one first “

light”

impurity and at least one second “

light”

impurity, said first “

light”

impurity being more volatile than said second “

light”

impurity.

13. The process of claim 1, wherein said “

light”

impurity depleted carbon dioxide bottoms liquid from said first column system is subcooled prior to being fed to said second column system.

14. The process of claim 1, wherein said “

light”

impurity depleted carbon dioxide bottoms liquid from said first column system is expanded prior to being fed to said second column system.

15. The process of claim 14, wherein said “

light”

impurity depleted carbon dioxide bottoms liquid from said first column system is subcooled by indirect heat exchange prior to being expanded.

16. The process of claim 1, wherein said “

light”

impurity depleted carbon dioxide bottoms liquid from said first column system is at least partially vaporized prior to being fed to said second column system.

17. The process of claim 16, wherein said “

light”

impurity depleted carbon dioxide bottoms liquid from said first column system is subcooled by indirect heat exchange and optionally expanded prior to being at least partially vaporized.

18. The process of claim 16, wherein said “

light”

impurity depleted carbon dioxide bottoms liquid from said first column system is expanded prior to being at least partially vaporized.

19. The process of claim 1, wherein said heat pump cycle comprises:

warming said carbon dioxide-enriched overhead vapor from said second column system by indirect heat exchange to produce a warmed carbon dioxide-enriched gas;

compressing said carbon dioxide-enriched gas to produce a compressed carbon dioxide-enriched recycle gas;

using said compressed carbon dioxide-enriched recycle gas to provide at least a part of the reboil duty required to vaporize said “

heavy”

impurity-enriched bottoms liquid thereby cooling and at least partially condensing said compressed carbon dioxide-enriched recycle gas to produce a carbon dioxide-enriched liquid;

expanding said carbon dioxide-enriched liquid to produce expanded carbon dioxide-enriched liquid; and

using at least a portion of said expanded carbon dioxide-enriched liquid to provide said reflux to said second column system.

20. The process of claim 1, wherein said “

light”

impurity-rich residual gas is warmed by indirect heat exchange and purged from said process.

21. The process of claim 1, wherein at least one “

light”

impurity is selected from the group consisting of hydrogen;

methane;

C₂ hydrocarbons; and

mixtures thereof, said “

light”

impurity-rich residual vapor being used as a fuel for combustion to produce combustion product gas.

22. The process of claim 21, wherein heat is recovered from said combustion product gas by indirect heat exchange.

23. The process of claim 1, wherein said crude carbon dioxide fluid comprises carbon dioxide in an amount of at least 50 mol %.

24. The process of claim 1, wherein said crude carbon dioxide fluid comprises said at least one “

light”

impurity in an amount of no more than 50 mol % in total.

25. The process of claim 1, wherein said crude carbon dioxide fluid comprises said at least one “

heavy”

impurity in an amount of no more than 50 mol % in total.

26. The process of claim 1 wherein at least one “

light”

impurity is selected from the group consisting of nitrogen;

oxygen;

argon;

neon;

xenon;

krypton;

carbon monoxide;

nitric oxide;

nitrous oxide;

hydrogen;

helium;

methane; and

C₂ hydrocarbons.

27. The process of claim 1, wherein at least one “

heavy”

impurity is selected from the group consisting of hydrogen sulfide;

methanol;

C₃ to C₈ hydrocarbons;

carbon disulfide;

carbon oxysulfide;

dimethyl sulfide and other organic sulfur compounds;

nitrogen dioxide, sulfur dioxide;

sulfur trioxide; and

ammonia.

28. The process of claim 1, wherein at least one “

heavy”

impurity is hydrogen sulfide.

29. The process of claim 28, wherein at least one “

light”

impurity is selected from the group consisting of nitrogen;

argon;

helium;

methane; and

ethane.

30. The process of claim 1, wherein the operating pressure(s) of said first column system is from 10 bar to 60 bar.

31. The process of claim 1, wherein the operating pressure(s) of said second column system is from 5.2 bar to 40 bar.

32. The process of claim 1, wherein the process is auto-refrigerated.

33. The process of claim 1, wherein the operating pressure(s) of said first column system is from 30 bar to 50 bar.

34. The process of claim 1, wherein the operating pressure(s) of said second column system is from 15 bar to 25 bar.