WO2015094175A1 - Purification of inert gases to remove trace impurities - Google Patents

Purification of inert gases to remove trace impurities Download PDF

Info

Publication number
WO2015094175A1
WO2015094175A1 PCT/US2013/075578 US2013075578W WO2015094175A1 WO 2015094175 A1 WO2015094175 A1 WO 2015094175A1 US 2013075578 W US2013075578 W US 2013075578W WO 2015094175 A1 WO2015094175 A1 WO 2015094175A1
Authority
WO
WIPO (PCT)
Prior art keywords
stream
argon
bottoms
distillation column
product stream
Prior art date
Application number
PCT/US2013/075578
Other languages
French (fr)
Inventor
Bao Ha
Daniel Gary
Purushottam V. Shanbhag
Original Assignee
L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude filed Critical L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude
Priority to PCT/US2013/075578 priority Critical patent/WO2015094175A1/en
Publication of WO2015094175A1 publication Critical patent/WO2015094175A1/en

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B23/00Noble gases; Compounds thereof
    • C01B23/001Purification or separation processes of noble gases
    • C01B23/0094Combined chemical and physical processing
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/08Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00Purification or separation of specific gases
    • C01B2210/0001Separation or purification processing
    • C01B2210/0003Chemical processing
    • C01B2210/0004Chemical processing by oxidation
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00Purification or separation of specific gases
    • C01B2210/0001Separation or purification processing
    • C01B2210/0009Physical processing
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00Purification or separation of specific gases
    • C01B2210/0001Separation or purification processing
    • C01B2210/0009Physical processing
    • C01B2210/0014Physical processing by adsorption in solids
    • C01B2210/0015Physical processing by adsorption in solids characterised by the adsorbent
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00Purification or separation of specific gases
    • C01B2210/0029Obtaining noble gases
    • C01B2210/0034Argon
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00Purification or separation of specific gases
    • C01B2210/0043Impurity removed
    • C01B2210/0045Oxygen
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00Purification or separation of specific gases
    • C01B2210/0043Impurity removed
    • C01B2210/0046Nitrogen
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00Purification or separation of specific gases
    • C01B2210/0043Impurity removed
    • C01B2210/005Carbon monoxide
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00Purification or separation of specific gases
    • C01B2210/0043Impurity removed
    • C01B2210/0051Carbon dioxide
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00Purification or separation of specific gases
    • C01B2210/0043Impurity removed
    • C01B2210/0053Hydrogen
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00Purification or separation of specific gases
    • C01B2210/0043Impurity removed
    • C01B2210/0062Water
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00Purification or separation of specific gases
    • C01B2210/0043Impurity removed
    • C01B2210/0068Organic compounds
    • C01B2210/007Hydrocarbons
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00Processes or apparatus using separation by rectification
    • F25J2200/02Processes or apparatus using separation by rectification in a single pressure main column system
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00Processes or apparatus using separation by rectification
    • F25J2200/04Processes or apparatus using separation by rectification in a dual pressure main column system
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00Processes or apparatus using separation by rectification
    • F25J2200/40Features relating to the provision of boil-up in the bottom of a column
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00Processes or apparatus using separation by rectification
    • F25J2200/50Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00Processes or apparatus using separation by rectification
    • F25J2200/72Refluxing the column with at least a part of the totally condensed overhead gas
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00Processes or apparatus using other separation and/or other processing means
    • F25J2205/40Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00Processes or apparatus using other separation and/or other processing means
    • F25J2205/60Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00Processes characterised by the type or other details of the feed stream
    • F25J2210/58Argon
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00Processes characterised by the type or other details of the product stream
    • F25J2215/58Argon
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2220/00Processes or apparatus involving steps for the removal of impurities
    • F25J2220/04Separating impurities in general from the product stream
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/06Lifting of liquids by gas lift, e.g. "Mammutpumpe"
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00Refrigeration techniques used
    • F25J2270/58Quasi-closed internal or closed external argon refrigeration cycle
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00Refrigeration techniques used
    • F25J2270/90External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

Definitions

  • the present invention relates to a system for the purification of inert gases. More specifically, the present disclosure relates to a system for the onsite removal of trace impurities, such as nitrogen and methane, from an argon stream using cryogenic distillation separation.
  • trace impurities such as nitrogen and methane
  • argon as an inert gas is important to a number of industries including the production of monocrystalline and polycrystalline silicon, steel making (e.g., using the hot isotatic pressing (HIP) process to make steel, aluminum and nonmetallic castings from powders), heat treating, and semiconductor, wafer, and electronics manufacturing.
  • HIP hot isotatic pressing
  • semiconductor, wafer, and electronics manufacturing Given the rising costs of argon gas, onsite purification of waste argon streams to recycle back to the manufacturing process is increasingly common.
  • One manufacturing process suitable for argon purification and recycle is the production of monocrystalline silicon using the Czochralski Process.
  • High purity argon i.e., having a purity of 99.999% or greater, is used in the process to control the atmosphere and to purge contaminants and volatilized materials from the process as a waste stream.
  • Purity of the argon stream is critical because it affects the both the purity and the quality of the silicon ingot grown in the Czochralski Process.
  • the waste stream from the process which may include between about 95 to about 99% argon (Ar), may contain any number of contaminants including: oxygen ((3 ⁇ 4), hydrogen (H 2 ), volatilized silicon oxide (SiO), carbon dioxide (CO 2 ), carbon monoxide (CO), nitrogen (N 2 ), water (H 2 0), methane (CH 4 ), other hydrocarbons, and other impurities.
  • oxygen ((3 ⁇ 4)
  • hydrogen hydrogen
  • SiO volatilized silicon oxide
  • CO 2 carbon dioxide
  • CO carbon monoxide
  • N 2 water
  • H 2 0 water
  • methane (CH 4 ) methane
  • Argon purification systems as described above, are available in packaged skids typically sold to companies for housing on their property for use in their manufacturing process.
  • current systems do not address methane slippage and are incapable of removing impurities below part per million (ppm) levels.
  • the present invention relates to a system for the purification of inert gases. More specifically, the present disclosure relates to a system for the onsite removal of trace impurities, such as nitrogen and methane, from an argon stream using cryogenic distillation separation.
  • trace impurities such as nitrogen and methane
  • an argon purification system includes a cryogenic heat exchanger configured to remove heat from a pre-treated argon waste stream to create a cold feed stream.
  • a cryogenic distillation column includes a reboiler and an overhead condenser, said column having an upper portion and a lower portion and is configured to receive a liquid feed stream and to produce a bottoms argon product stream and a gas waste stream.
  • the reboiler is positioned in the lower portion of the cryogenic distillation column and is configured to remove heat from the cold feed stream such that the cold feed stream condenses to the liquid feed stream.
  • the condenser is positioned in the upper portion of the cryogenic distillation column and is configured to heat the bottoms argon product stream such that the bottoms argon product stream evaporates to a purified vapor phase argon stream.
  • the cryogenic heat exchanger heats the purified vapor phase argon stream with the heat removed from the pre-treated argon waste stream. In certain embodiments, the cryogenic heat exchanger heats the gas waste stream with the heat removed from the pre-treated argon waste stream. In certain embodiments, the reboiler uses the heat removed from a cryogenic distillation column overheads to heat the bottoms argon product stream. In certain embodiments, the overhead condenser uses heat removed from the cryogenic distillation column overheads to heat the bottoms argon product stream.
  • the bottoms argon product stream undergoes expansion in an expansion device before being fed to the overhead condenser, such that the temperature of the bottoms argon product stream is reduced in the expansion device.
  • a pump provides the driving force to get the bottoms argon product stream to the overhead condenser.
  • the cryogenic distillation column is configured with additional stages above the overhead condenser.
  • the argon purification system includes a sorbent bed system, such that the sorbent bed system accepts the bottoms argon product stream, removes contaminants from the bottoms argon product stream, and then feeds a sorbent bed outlet stream to the overhead condenser.
  • the sorbent bed system is filled with regenerable adsorbents.
  • the sorbent bed system is filled with getter materials.
  • FIG. 1 shows one preferred embodiment of the invention.
  • FIG. 2 shows another preferred embodiment of the invention.
  • FIG. 3 shows an alternative preferred embodiment of the invention.
  • FIG. 4 shows another preferred embodiment of the invention. Detailed Description
  • the present invention describes a cryogenic distillation system capable of removing trace impurities from an argon stream.
  • FIG. 1 provides an illustration of an embodiment of the present invention.
  • Pre-treated argon waste stream 2 is the outlet of the pre-treatment process.
  • the waste gas stream from the manufacturing process will include argon, H 2 , (3 ⁇ 4, CO 2, CO, CH 4 , and H 2 0, along with other trace impurities.
  • the pre-treatment process begins by compressing the waste gas stream.
  • the compressed gas is then fed, along with excess O 2 and H 2 , or air, if necessary, to a series of commercially available catalyst beds that oxidize CO, CH 4 , and O2 to CO2 and H2O.
  • the CO2 and H 2 O are removed by adsorption, either by using molecular-sieve or a combination of silica gel and molecular-sieve, resulting in pre-treated argon waste gas stream 2.
  • Pre-treated argon waste stream 2 contains greater than about 95% argon, less than about 4% N 2 , less than about 1% H 2 , less than about 1 ppm H 2 , 0 2 , CO, and CH 4 , and no CO 2 or H2O.
  • the exact temperature, pressure and composition of pre-treated argon waste stream 2 will depend on the specific manufacturing and pre-treatment processes that are employed. In certain embodiments, the pre-treatment process removes as much O 2 , CO, and CH 4 as possible, to achieve concentrations from about 1 ppm to 10 ppm, alternatively to below 1 ppm.
  • Pre-treated argon waste stream 2 is fed into cryogenic heat exchanger 10, where it is cooled to a temperature between about -150°C and -160°C, alternatively between about - 152°C and -157°C, alternatively between about -153°C and -155°C, alternatively about - 153.6°C.
  • Cryogenic heat exchanger 10 may be any heat exchanger of the type and materials commonly employed in a cryogenic air separation process. In certain embodiments, the heat exchanger is constructed of brazed aluminum.
  • Cold feed stream 12 exits cryogenic heat exchanger 10 and enters reboiler 30. Additional energy is removed from cold feed stream 12 in reboiler 30, and the heat from cold feed stream 12 is used to provide reboil liquid at the bottom of column 20. This results in condensing of cold feed stream 12.
  • Liquid feed stream 32 exits reboiler 30 at a temperature between about -150°C to about -160°C, preferably about -156.9°C. Liquid feed stream 32 is then fed to cryogenic distillation column 20 at a point above the bottom section and below the upper section, preferably in the packing section.
  • Argon stream 4 is fed to cryogenic distillation column 20 to make up for argon lost as waste in gaseous waste stream 26 and the liquid purge 28. Any refrigeration requirements for the process such as heat leakage, temperature differences in heat exchanger 10, liquid purge or other losses can be compensated by the addition of argon stream 4.
  • Argon stream 4 is a high purity source of liquid argon containing at least about 99.999% argon, less than about 0.001% (3 ⁇ 4, and less than about 0.001% N 2 .
  • argon feed stream 4 can also provide additional cooling for cryogenic distillation column 20. The temperature of argon feed stream 4 is preferably close to its dew point.
  • Bottoms argon product stream 22 exits cryogenic distillation column 20. Bottoms argon product stream 22 has a purity of at least about 99.999% argon. After exiting cryogenic distillation column 20, bottoms argon product stream 22 is cooled by expansion in expansion device 50. Expansion device 50 may be any device capable of reducing the pressure and temperature of bottoms argon product stream 50. In one embodiment, bottoms argon product stream 22 is cooled to at or about its bubble point.
  • Bottoms argon product stream 22 can be supplied to overhead condenser 40.
  • argon lift stream 6 (a small stream of argon gas, less than about 1% by mass of bottoms argon product stream 22) can be added to bottoms argon product stream 22 after expansion valve 50 as a lift gas to drive the stream to overhead condenser 40.
  • This feature can be useful to ease the liquid transfer when distillation column 20 is tall, particularly due to the relatively high density of liquid argon and the low differential pressure between the bottom of distillation column 20 and overhead condenser 40.
  • a partial vapor stream that includes argon lift stream 6 and bottoms argon product stream 22 i.e., bottoms lift stream 52), operates by virtue of the buoyancy of a gas-liquid slug.
  • Bottoms lift stream 52 provides cooling to overhead condenser 40, which vaporizes bottoms lift stream 52 to create purified vapor phase argon stream 24. Vapor from the top of cryogenic distillation column 20 partially condenses in overhead condenser 40 due to the cooling provided by bottoms lift stream 52. A small liquid purge stream 28 containing some heavy impurities such as hydrocarbons, carbon dioxide, etc... can be removed from overhead condenser 40.
  • Purified vapor phase argon stream 24 can be fed to cryogenic heat exchanger 10 to provide cooling for pre-treated argon waste stream 2.
  • Product stream 14, having a temperature of about ambient temperature, may be returned to the manufacturing process requiring pure argon, may be stored, may be diverted for other processes, or may be distributed off-site. The purity of product stream 14 is greater than about 99.999% argon.
  • Nitrogen and 3 ⁇ 4 being more volatile than argon, collect near the top of cryogenic distillation column 20 and are removed from the distillation column as gaseous waste stream 26.
  • Gaseous waste stream 26 can be supplied to cryogenic heat exchanger 10 to provide cooling of pre-treated argon waste stream 2.
  • Warm gas waste stream 16 may then be recycled to the manufacturing process, disposed of, or used to regenerate the mole-sieve beds of the pre-treatment process.
  • a pump (not shown) can be used to supply the driving force to drive bottoms argon product stream 22 to overhead condenser 40.
  • the pump may be of any type and materials commonly used in a cryogenic distillation system.
  • argon lift stream 6 is not used when the pump is used.
  • FIG. 2 demonstrates an additional embodiment of the invention.
  • additional separation stages can been included in cryogenic distillation column 20 above overhead condenser 40.
  • the additional separation stages allow for further purification of the argon stream by removing CH 4 not removed during the pre-treatment process, thus addressing methane slippage. Methane, which is less volatile than argon, will be carried out the bottom of cryogenic distillation column 20 in bottoms argon product stream 22.
  • the additional stages in cryogenic distillation column 20 allow for the separation and removal of this CH 4 prior to purified vapor phase argon stream 24 exiting cryogenic distillation column 20.
  • Methane waste stream 28 may be bled from the column below the additional stages and disposed of or redirected as necessary.
  • the flowrate of argon stream 4 can be adjusted to account for additional argon losses in methane waste stream 28.
  • FIG. 3 illustrates an alternative embodiment of the invention.
  • a portion of product stream 14 can be diverted to compressor 60 through recycle stream 15.
  • Compressor 60 compresses recycle stream 15 to the pressure of cryogenic distillation column 20, creating compressed argon recycle stream 68.
  • Compressed stream 68 can be fed to cryogenic heat exchanger 10 to be cooled.
  • the cooled and compressed argon recycle stream 18 is cooled to a temperature at or about its dew point, and is fed to cryogenic distillation column 20.
  • Between about 5 and 25% of product stream 14 by volume can be recycled to cryogenic distillation column 20 to improve the overall recovery of argon.
  • between about 5 and 10% by volume is recycled, alternatively between about 10 and 15% by volume, alternatively between about 15 and 20% by volume, alternatively between about 20 and 25%.
  • by recycling approximately 10% of product stream 14 to cryogenic distillation column 20 can increase overall argon recovery from about 83% to greater than 90%, alternatively greater than 95%, alternatively to about 99%.
  • FIG. 4 illustrates yet another embodiment of the invention.
  • bottoms argon product stream 22 can be supplied to sorbent bed system 80 to reduce contaminants in bottoms argon product stream 22.
  • Pump 70 can provide the drive necessary so sorbent bed feed stream 72 can pass through sorbent bed system 80 and can enter overhead condenser 40.
  • Sorbent bed system 80 can include two or more beds in parallel, or alternatively can include two or more beds such that at least one is a back-up for use when another bed is being serviced.
  • Sorbent bed system 80 may be filled with regenerable adsorbents or nonregenerable getter materials.
  • Getter materials can include finely divided metals (such as, for example, zirconium, tantalum, copper, nickel, etc.) on a substrate, such as alumina, ceria or kieselguhr.
  • sorbent bed system 80 will remove contaminants such that the concentration of CO, CH 4 , H 2 , O2, N 2 , and H 2 0 is reduced to between about 1 ppm to about 10 ppm, alternatively to between about 1 ppb to 10 ppb.
  • Outlet stream 82 from sorbent bed system 80 may be returned to overhead condenser 40, or alternatively may be diverted for other processes.
  • Table 1 provides data for a representative process, utilizing the embodiment illustrated in FIG. 1.
  • the manufacturing process pre-treated argon gas waste stream is provided from a monocrystalline silicon production process. A molar gas flowrate of 500 m 3 /h was chosen for simulation purposes.
  • the process conditions of pre-treated argon waste stream 2 are based on the outlet of a pre-treatment process, which typically takes place at an ambient temperature, but with a compressed gas stream, thus for simulation purposes an inlet temperature of 20°C and 147 psig were chosen.
  • the composition of pre-treated argon waste stream 2 assumes some CH 4 leakage and impurities of CO and O2 on the part per million scale.
  • the present invention is capable of removing trace impurities to produce an argon stream (product stream 14), having an argon purity of greater than 99.999%.
  • Cold feed stream 12 leaving cryogenic heat exchanger 10 was cooled to a temperature of -153.6°C by using the cold from purified vapor phase argon stream 24 and gaseous waste stream 26.
  • Providing in a claim is defined to mean furnishing, supplying, making available, or preparing something. The step may be performed by any actor in the absence of express language in the claim to the contrary a range is expressed, it is to be understood that another embodiment is from the one.
  • Optional or optionally means that the subsequently described event or circumstances may or may not occur.
  • the description includes instances where the event or circumstance occurs and instances where it does not occur.
  • Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such particular value and/or to the other particular value, along with all combinations within said range.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

An argon purification system is provided which includes a cryogenic heat exchanger, a cryogenic distillation column. The cryogenic heat exchanger is configured to remove heat from a pre-treated argon waste stream to create a cold feed stream. The cryogenic distillation column includes packing, a reboiler, and an overhead condenser, as well as an upper portion and a lower portion and is configured to receive a liquid feed stream and to produce a bottoms argon product stream and a gas waste stream. The reboiler is positioned in the lower portion of the cryogenic distillation column and is configured to condense the cold feed stream to produce the liquid feed stream. The condenser is positioned in the upper portion of the cryogenic distillation column and is configured to heat the bottoms argon product stream such that the bottoms argon product stream evaporates to a purified vapor phase argon stream.

Description

PURIFICATION OF INERT GASES TO REMOVE TRACE IMPURITIES Technical Field of Invention
[0001] The present invention relates to a system for the purification of inert gases. More specifically, the present disclosure relates to a system for the onsite removal of trace impurities, such as nitrogen and methane, from an argon stream using cryogenic distillation separation.
Background of the Invention
[0002] The use of argon as an inert gas is important to a number of industries including the production of monocrystalline and polycrystalline silicon, steel making (e.g., using the hot isotatic pressing (HIP) process to make steel, aluminum and nonmetallic castings from powders), heat treating, and semiconductor, wafer, and electronics manufacturing. Given the rising costs of argon gas, onsite purification of waste argon streams to recycle back to the manufacturing process is increasingly common.
[0003] One manufacturing process suitable for argon purification and recycle is the production of monocrystalline silicon using the Czochralski Process. High purity argon, i.e., having a purity of 99.999% or greater, is used in the process to control the atmosphere and to purge contaminants and volatilized materials from the process as a waste stream. Purity of the argon stream is critical because it affects the both the purity and the quality of the silicon ingot grown in the Czochralski Process.
[0004] The waste stream from the process, which may include between about 95 to about 99% argon (Ar), may contain any number of contaminants including: oxygen ((¾), hydrogen (H2), volatilized silicon oxide (SiO), carbon dioxide (CO2), carbon monoxide (CO), nitrogen (N2), water (H20), methane (CH4), other hydrocarbons, and other impurities. Although commercial technologies currently address the removal of contaminants such as (¾, H2, CO2, CO, H20, and hydrocarbons, cryogenic distillation is still the preferred route for the removal of N2 and CH4.
[0005] Current methods for the purification of argon typically utilize a cryogenic distillation process used in conjunction with a pre-treatment process. Current pre-treatment process systems begin by compressing the waste stream. The compressed gas is fed, along with excess O2 and ¾ if necessary, to a series of commercially available catalyst beds that oxidize CO and CH4 to CO2 and H20. The CO2 and H20 can be removed by adsorption, either by using molecular-sieve or a combination of silica gel and molecular-sieve. The waste stream now contains primarily argon, N2, and ¾, and may also contain minute quantities of CH4 (methane slippage), which must be removed prior to recycle to the manufacturing process. With the CO2 and ¾0 removed, the argon waste stream may be fed to a cryogenic distillation system capable of removing the N2, any remaining ¾.
[0006] Argon purification systems, as described above, are available in packaged skids typically sold to companies for housing on their property for use in their manufacturing process. However, current systems do not address methane slippage and are incapable of removing impurities below part per million (ppm) levels.
[0007] Therefore, it would be beneficial to have a simpler cryogenic distillation system with fewer mechanical parts. Additional benefits could be gained if a simpler system was capable of removing more impurities and addressing methane slippage from the pre-treatment process. Summary of the Invention
[0008] The present invention relates to a system for the purification of inert gases. More specifically, the present disclosure relates to a system for the onsite removal of trace impurities, such as nitrogen and methane, from an argon stream using cryogenic distillation separation.
[0009] In one embodiment, an argon purification system is provided. The argon purification system includes a cryogenic heat exchanger configured to remove heat from a pre-treated argon waste stream to create a cold feed stream. A cryogenic distillation column includes a reboiler and an overhead condenser, said column having an upper portion and a lower portion and is configured to receive a liquid feed stream and to produce a bottoms argon product stream and a gas waste stream. The reboiler is positioned in the lower portion of the cryogenic distillation column and is configured to remove heat from the cold feed stream such that the cold feed stream condenses to the liquid feed stream. The condenser is positioned in the upper portion of the cryogenic distillation column and is configured to heat the bottoms argon product stream such that the bottoms argon product stream evaporates to a purified vapor phase argon stream.
[0010] In certain embodiments, the cryogenic heat exchanger heats the purified vapor phase argon stream with the heat removed from the pre-treated argon waste stream. In certain embodiments, the cryogenic heat exchanger heats the gas waste stream with the heat removed from the pre-treated argon waste stream. In certain embodiments, the reboiler uses the heat removed from a cryogenic distillation column overheads to heat the bottoms argon product stream. In certain embodiments, the overhead condenser uses heat removed from the cryogenic distillation column overheads to heat the bottoms argon product stream. In certain embodiments, the bottoms argon product stream undergoes expansion in an expansion device before being fed to the overhead condenser, such that the temperature of the bottoms argon product stream is reduced in the expansion device. In certain embodiments, a pump provides the driving force to get the bottoms argon product stream to the overhead condenser.
[0011] In certain embodiments, the cryogenic distillation column is configured with additional stages above the overhead condenser. In certain embodiments, the argon purification system includes a sorbent bed system, such that the sorbent bed system accepts the bottoms argon product stream, removes contaminants from the bottoms argon product stream, and then feeds a sorbent bed outlet stream to the overhead condenser. In certain embodiments, the sorbent bed system is filled with regenerable adsorbents. In certain embodiments, the sorbent bed system is filled with getter materials.
Brief Description of the Drawings
[0012] These and other features, aspects, and advantages of the present invention will become better understood with regard to the following description, claims, and accompanying drawings. It is to be noted, however, that the drawings illustrate only several embodiments of the invention and are therefore not to be considered limiting of the invention's scope as it can admit to other equally effective embodiments.
[0013] FIG. 1 shows one preferred embodiment of the invention.
[0014] FIG. 2 shows another preferred embodiment of the invention.
[0015] FIG. 3 shows an alternative preferred embodiment of the invention.
[0016] FIG. 4 shows another preferred embodiment of the invention. Detailed Description
[0017] While the invention will be described with several embodiments, it is understood that one of ordinary skill in the relevant art will appreciate that many examples variations, and alterations to the following details are within the scope and spirit of the invention. Accordingly, the exemplary embodiments of the invention described herein are set forth without any loss of generality, and without imposing limitations, relating to the claimed invention.
[0018] In one embodiment, the present invention describes a cryogenic distillation system capable of removing trace impurities from an argon stream.
[0019] FIG. 1 provides an illustration of an embodiment of the present invention. Pre-treated argon waste stream 2 is the outlet of the pre-treatment process. The waste gas stream from the manufacturing process will include argon, H2, (¾, CO2, CO, CH4, and H20, along with other trace impurities. The pre-treatment process begins by compressing the waste gas stream. The compressed gas is then fed, along with excess O2 and H2, or air, if necessary, to a series of commercially available catalyst beds that oxidize CO, CH4, and O2 to CO2 and H2O. The CO2 and H2O are removed by adsorption, either by using molecular-sieve or a combination of silica gel and molecular-sieve, resulting in pre-treated argon waste gas stream 2.
[0020] Pre-treated argon waste stream 2 contains greater than about 95% argon, less than about 4% N2, less than about 1% H2, less than about 1 ppm H2, 02, CO, and CH4, and no CO2 or H2O. The exact temperature, pressure and composition of pre-treated argon waste stream 2 will depend on the specific manufacturing and pre-treatment processes that are employed. In certain embodiments, the pre-treatment process removes as much O2, CO, and CH4 as possible, to achieve concentrations from about 1 ppm to 10 ppm, alternatively to below 1 ppm. [0021] Pre-treated argon waste stream 2 is fed into cryogenic heat exchanger 10, where it is cooled to a temperature between about -150°C and -160°C, alternatively between about - 152°C and -157°C, alternatively between about -153°C and -155°C, alternatively about - 153.6°C. Cryogenic heat exchanger 10 may be any heat exchanger of the type and materials commonly employed in a cryogenic air separation process. In certain embodiments, the heat exchanger is constructed of brazed aluminum.
[0022] Cold feed stream 12 exits cryogenic heat exchanger 10 and enters reboiler 30. Additional energy is removed from cold feed stream 12 in reboiler 30, and the heat from cold feed stream 12 is used to provide reboil liquid at the bottom of column 20. This results in condensing of cold feed stream 12. Liquid feed stream 32 exits reboiler 30 at a temperature between about -150°C to about -160°C, preferably about -156.9°C. Liquid feed stream 32 is then fed to cryogenic distillation column 20 at a point above the bottom section and below the upper section, preferably in the packing section.
[0023] Argon stream 4 is fed to cryogenic distillation column 20 to make up for argon lost as waste in gaseous waste stream 26 and the liquid purge 28. Any refrigeration requirements for the process such as heat leakage, temperature differences in heat exchanger 10, liquid purge or other losses can be compensated by the addition of argon stream 4. In one embodiment, Argon stream 4 is a high purity source of liquid argon containing at least about 99.999% argon, less than about 0.001% (¾, and less than about 0.001% N2. Advantageously, argon feed stream 4 can also provide additional cooling for cryogenic distillation column 20. The temperature of argon feed stream 4 is preferably close to its dew point.
[0024] Bottoms argon product stream 22 exits cryogenic distillation column 20. Bottoms argon product stream 22 has a purity of at least about 99.999% argon. After exiting cryogenic distillation column 20, bottoms argon product stream 22 is cooled by expansion in expansion device 50. Expansion device 50 may be any device capable of reducing the pressure and temperature of bottoms argon product stream 50. In one embodiment, bottoms argon product stream 22 is cooled to at or about its bubble point.
[0025] Bottoms argon product stream 22 can be supplied to overhead condenser 40. In one embodiment, argon lift stream 6 (a small stream of argon gas, less than about 1% by mass of bottoms argon product stream 22) can be added to bottoms argon product stream 22 after expansion valve 50 as a lift gas to drive the stream to overhead condenser 40. This feature can be useful to ease the liquid transfer when distillation column 20 is tall, particularly due to the relatively high density of liquid argon and the low differential pressure between the bottom of distillation column 20 and overhead condenser 40. A partial vapor stream that includes argon lift stream 6 and bottoms argon product stream 22 (i.e., bottoms lift stream 52), operates by virtue of the buoyancy of a gas-liquid slug.
[0026] Bottoms lift stream 52 provides cooling to overhead condenser 40, which vaporizes bottoms lift stream 52 to create purified vapor phase argon stream 24. Vapor from the top of cryogenic distillation column 20 partially condenses in overhead condenser 40 due to the cooling provided by bottoms lift stream 52. A small liquid purge stream 28 containing some heavy impurities such as hydrocarbons, carbon dioxide, etc... can be removed from overhead condenser 40.
[0027] Purified vapor phase argon stream 24 can be fed to cryogenic heat exchanger 10 to provide cooling for pre-treated argon waste stream 2. Product stream 14, having a temperature of about ambient temperature, may be returned to the manufacturing process requiring pure argon, may be stored, may be diverted for other processes, or may be distributed off-site. The purity of product stream 14 is greater than about 99.999% argon. [0028] Nitrogen and ¾, being more volatile than argon, collect near the top of cryogenic distillation column 20 and are removed from the distillation column as gaseous waste stream 26. Gaseous waste stream 26 can be supplied to cryogenic heat exchanger 10 to provide cooling of pre-treated argon waste stream 2. Warm gas waste stream 16 may then be recycled to the manufacturing process, disposed of, or used to regenerate the mole-sieve beds of the pre-treatment process.
[0029] In a second embodiment of the system in FIG. 1, a pump (not shown) can be used to supply the driving force to drive bottoms argon product stream 22 to overhead condenser 40. The pump may be of any type and materials commonly used in a cryogenic distillation system. In one embodiment, argon lift stream 6 is not used when the pump is used.
[0030] FIG. 2 demonstrates an additional embodiment of the invention. In this embodiment, in addition to the features shown in FIG. 1 and described above, additional separation stages can been included in cryogenic distillation column 20 above overhead condenser 40. The additional separation stages allow for further purification of the argon stream by removing CH4 not removed during the pre-treatment process, thus addressing methane slippage. Methane, which is less volatile than argon, will be carried out the bottom of cryogenic distillation column 20 in bottoms argon product stream 22. The additional stages in cryogenic distillation column 20 allow for the separation and removal of this CH4 prior to purified vapor phase argon stream 24 exiting cryogenic distillation column 20. Methane waste stream 28 may be bled from the column below the additional stages and disposed of or redirected as necessary. The flowrate of argon stream 4 can be adjusted to account for additional argon losses in methane waste stream 28. It is understood that the additional separation stages shown in Figure 2 can also be added to the additional embodiments described herein, for example FIG. 3 and FIG. 4. [0031] FIG. 3 illustrates an alternative embodiment of the invention. In this embodiment, in addition to the features shown in FIG. 1 and described above, a portion of product stream 14 can be diverted to compressor 60 through recycle stream 15. Compressor 60 compresses recycle stream 15 to the pressure of cryogenic distillation column 20, creating compressed argon recycle stream 68. Compressed stream 68 can be fed to cryogenic heat exchanger 10 to be cooled. The cooled and compressed argon recycle stream 18 is cooled to a temperature at or about its dew point, and is fed to cryogenic distillation column 20. Between about 5 and 25% of product stream 14 by volume can be recycled to cryogenic distillation column 20 to improve the overall recovery of argon. In alternate embodiments, between about 5 and 10% by volume is recycled, alternatively between about 10 and 15% by volume, alternatively between about 15 and 20% by volume, alternatively between about 20 and 25%. In certain embodiments, by recycling approximately 10% of product stream 14 to cryogenic distillation column 20 can increase overall argon recovery from about 83% to greater than 90%, alternatively greater than 95%, alternatively to about 99%.
[0032] FIG. 4 illustrates yet another embodiment of the invention. In this embodiment, in addition to the features shown in FIG. 1 and FIG. 3 and described above, bottoms argon product stream 22 can be supplied to sorbent bed system 80 to reduce contaminants in bottoms argon product stream 22. Pump 70 can provide the drive necessary so sorbent bed feed stream 72 can pass through sorbent bed system 80 and can enter overhead condenser 40.
[0033] Sorbent bed system 80 can include two or more beds in parallel, or alternatively can include two or more beds such that at least one is a back-up for use when another bed is being serviced. Sorbent bed system 80 may be filled with regenerable adsorbents or nonregenerable getter materials. Getter materials can include finely divided metals (such as, for example, zirconium, tantalum, copper, nickel, etc.) on a substrate, such as alumina, ceria or kieselguhr. In certain embodiments, sorbent bed system 80 will remove contaminants such that the concentration of CO, CH4, H2, O2, N2, and H20 is reduced to between about 1 ppm to about 10 ppm, alternatively to between about 1 ppb to 10 ppb. Outlet stream 82 from sorbent bed system 80 may be returned to overhead condenser 40, or alternatively may be diverted for other processes.
Example 1:
[0034] The present invention is further demonstrated by the following illustrative embodiment, which does not limit the claims of the present invention.
[0035] Table 1 provides data for a representative process, utilizing the embodiment illustrated in FIG. 1. The manufacturing process pre-treated argon gas waste stream is provided from a monocrystalline silicon production process. A molar gas flowrate of 500 m3/h was chosen for simulation purposes. The process conditions of pre-treated argon waste stream 2 are based on the outlet of a pre-treatment process, which typically takes place at an ambient temperature, but with a compressed gas stream, thus for simulation purposes an inlet temperature of 20°C and 147 psig were chosen. Finally, the composition of pre-treated argon waste stream 2 assumes some CH4 leakage and impurities of CO and O2 on the part per million scale.
Table 1: Representative Data
Figure imgf000012_0001
[0036] As shown in Table 1, the present invention is capable of removing trace impurities to produce an argon stream (product stream 14), having an argon purity of greater than 99.999%. Cold feed stream 12 leaving cryogenic heat exchanger 10 was cooled to a temperature of -153.6°C by using the cold from purified vapor phase argon stream 24 and gaseous waste stream 26.
[0037] While the invention has been described in conjunction with specific embodiments thereof, it is evident that many alternatives, modifications, and variations will be apparent to those skilled in the art in light of the foregoing description. Accordingly, it is intended to embrace all such alternatives, modifications, and variations as fall within the spirit and broad scope of the appended claims. The present invention may suitably comprise, consist or consist essentially of the elements disclosed and may be practiced in the absence of an element not disclosed. Furthermore, if there is language referring to order, such as first and second, it should be understood in an exemplary sense and not in a limiting sense. For example, it can be recognized by those skilled in the art that certain steps can be combined into a single step.
[0038] The singular forms "a", "an" and "the" include plural referents, unless the context clearly dictates otherwise. [0039] "Comprising" in a claim is an open transitional term which means the subsequently identified claim elements are a nonexclusive listing (i.e., anything else may be additionally included and remain within the scope of "comprising"). "Comprising" as used herein may be replaced by the more limited transitional terms "consisting essentially of and "consisting of unless otherwise indicated herein.
[0040] "Providing" in a claim is defined to mean furnishing, supplying, making available, or preparing something. The step may be performed by any actor in the absence of express language in the claim to the contrary a range is expressed, it is to be understood that another embodiment is from the one.
[0041] Optional or optionally means that the subsequently described event or circumstances may or may not occur. The description includes instances where the event or circumstance occurs and instances where it does not occur.
[0042] Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such particular value and/or to the other particular value, along with all combinations within said range.
[0043] All references identified herein are each hereby incorporated by reference into this application in their entireties, as well as for the specific information for which each is cited.

Claims

CLAIMS What is claimed is:
1. An argon purification system, the system comprising: a cryogenic heat exchanger, wherein the cryogenic heat exchanger is configured to remove heat from a pre-treated argon waste stream to create a cold feed stream; a cryogenic distillation column comprising a packing section, a reboiler, and an overhead condenser, said cryogenic distillation column having an upper portion and a lower portion and being configured to receive a liquid feed stream and to produce a bottoms argon product stream and a gas waste stream; wherein the reboiler is positioned in the lower portion of the cryogenic distillation column and is configured to remove heat from the cold feed stream such that the cold feed stream condenses to the liquid feed stream; and wherein the overhead condenser is positioned in the upper portion of the cryogenic distillation column and is configured to heat the bottoms argon product stream such that the bottoms argon product stream evaporates to a purified vapor phase argon stream.
2. The system as claimed in any of the preceding claims, wherein the cryogenic heat exchanger is further configured to heat the purified vapor phase argon stream with the heat removed from the pre-treated argon waste stream.
3. The system as claimed in any of the preceding claims, wherein the cryogenic heat exchanger is further configured to heat the gas waste stream with the heat removed from the pre-treated argon waste stream.
4. The system as claimed in any of the preceding claims, wherein the reboiler is configured to use the heat removed from the cold feed stream to boil the liquid in a cryogenic distillation column bottoms.
5. The system as claimed in any of the preceding claims, wherein the overhead condenser is configured to use heat removed from a cryogenic distillation column overheads to heat the bottoms argon product stream.
6. The system as claimed in any of the preceding claims, further comprising an expansion device in fluid communication with the bottom portion of the cryogenic distillation column, the expansion device configured to receive and expand the bottoms argon product stream before the bottoms argon product stream is fed to the overhead condenser, such that the temperature of the bottoms argon product stream is reduced.
7. The system as claimed in any of the preceding claims, further comprising a pump that is configured to provide a driving force to get the bottoms argon product stream to the overhead condenser.
8. The system as claimed in any of the preceding claims, further comprising an argon lift stream in fluid communication with the bottoms argon product stream, the argon lift stream configured to provide additional lift to the bottoms argon product stream by introducing gaseous argon into the bottoms argon product stream.
9. The system as claimed in Claim 8, wherein the argon lift stream is less than about 1% by mass of the bottoms argon product stream.
10. The system as claimed in any of the preceding claims, wherein the cryogenic distillation column further comprises additional stages disposed above the overhead condenser configured to remove methane from the bottoms argon product stream.
11. The system as claimed in any of the preceding claims, further comprising a sorbent bed system, wherein the sorbent bed system is configured to accept the bottoms argon product stream, to remove contaminants from the bottoms argon product stream to produce a sorbent bed outlet stream, and then feed the sorbent bed outlet stream to the overhead condenser.
12. The system as claimed in Claim 1 1, wherein the sorbent bed system is filled with regenerable adsorbents.
13. The system as claimed in Claim 1 1, wherein the sorbent bed system is filled with getter materials.
14. The system as claimed in any of the preceding claims, wherein the pre-treated argon waste stream is sourced from a monocrystalline silicon production process.
15. The system as claimed in any of the preceding claims, further comprising a recycle compressor in fluid communication with the heat exchanger, the purified vapor phase argon stream, and the cryogenic distillation column, wherein the recycle compressor is configured to compress a portion of the purified vapor phase argon stream to produce a compressed argon recycle, wherein the heat exchanger is configured to cool the compressed argon recycle before introducing the compressed argon recycle into the cryogenic distillation column for further purification.
PCT/US2013/075578 2013-12-17 2013-12-17 Purification of inert gases to remove trace impurities WO2015094175A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/US2013/075578 WO2015094175A1 (en) 2013-12-17 2013-12-17 Purification of inert gases to remove trace impurities

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/US2013/075578 WO2015094175A1 (en) 2013-12-17 2013-12-17 Purification of inert gases to remove trace impurities

Publications (1)

Publication Number Publication Date
WO2015094175A1 true WO2015094175A1 (en) 2015-06-25

Family

ID=49917274

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2013/075578 WO2015094175A1 (en) 2013-12-17 2013-12-17 Purification of inert gases to remove trace impurities

Country Status (1)

Country Link
WO (1) WO2015094175A1 (en)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106288653A (en) * 2016-10-21 2017-01-04 上海跃绅能源科技有限公司 A kind of single column cryogenic rectification reclaims device and the method for purification recovery argon of argon
CN110368709A (en) * 2019-07-05 2019-10-25 苏州市兴鲁空分设备科技发展有限公司 Argon device for recovering tail gas
WO2020025214A1 (en) * 2018-07-28 2020-02-06 Messer Group Gmbh Method for recycling argon
US20230392862A1 (en) * 2022-06-07 2023-12-07 Neil M. Prosser Krypton recovery and purification from customer processing

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19708025A1 (en) * 1996-02-28 1997-09-04 Air Prod & Chem Recovery and purification of argon from silicon crystal growing oven
WO2002095309A1 (en) * 2001-05-22 2002-11-28 Praxair Technology, Inc. Cryogenic system for producing high purity argon
WO2010139905A2 (en) * 2009-06-05 2010-12-09 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process and plant for recovering argon in a separation unit for a purge gas used in the synthesis of ammonia

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19708025A1 (en) * 1996-02-28 1997-09-04 Air Prod & Chem Recovery and purification of argon from silicon crystal growing oven
WO2002095309A1 (en) * 2001-05-22 2002-11-28 Praxair Technology, Inc. Cryogenic system for producing high purity argon
WO2010139905A2 (en) * 2009-06-05 2010-12-09 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process and plant for recovering argon in a separation unit for a purge gas used in the synthesis of ammonia

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106288653A (en) * 2016-10-21 2017-01-04 上海跃绅能源科技有限公司 A kind of single column cryogenic rectification reclaims device and the method for purification recovery argon of argon
WO2020025214A1 (en) * 2018-07-28 2020-02-06 Messer Group Gmbh Method for recycling argon
CN110368709A (en) * 2019-07-05 2019-10-25 苏州市兴鲁空分设备科技发展有限公司 Argon device for recovering tail gas
US20230392862A1 (en) * 2022-06-07 2023-12-07 Neil M. Prosser Krypton recovery and purification from customer processing

Similar Documents

Publication Publication Date Title
CA2893197C (en) Argon production method and apparatus
AU2019226284B2 (en) Helium extraction from natural gas
CA2822274C (en) Systems and methods for recovering helium from feed streams containing carbon dioxide
CA2618835A1 (en) Purification of carbon dioxide
WO1986004979A1 (en) Apparatus for producing high-purity nitrogen and oxygen gases
EP2002190A2 (en) Carbon dioxide purification method
JPS62228862A (en) Recovery of argon from purge gas of ammonia plant after discharge of hydrogen utilizing combination of low-temperature separation and non-low temperature separation
WO1999011437A1 (en) Method and apparatus for purification of argon
JPH04222381A (en) Manufacture of high-purity argon
MX2011010173A (en) Cyrogenic separation of synthesis gas.
AU2019226280A1 (en) Helium extraction from natural gas
WO2014132751A1 (en) Air separation method and air separation apparatus
US10197328B2 (en) Method and apparatus for purifying a carbon dioxide-rich mixture at a low temperature
CN108645118B (en) Device and method for improving argon recovery rate
WO2015094175A1 (en) Purification of inert gases to remove trace impurities
US20130298600A1 (en) Process and apparatus for production of ammonia synthesis gas and pure methane by cryogenic separation
WO1986000694A1 (en) Apparatus for producing high-purity nitrogen gas
WO2014099848A2 (en) Purification of inert gases to remove trace impurities
US20210080175A1 (en) Method and apparatus for the cryogenic separation of a synthesis gas containing a nitrogen separation step
EP3067315B1 (en) Light gas separation process and system
CN110803689A (en) Argon recovery method and device for removing carbon monoxide and integrating high-purity nitrogen by rectification method
JP2636949B2 (en) Improved nitrogen generator
US20140165649A1 (en) Purification of inert gases to remove trace impurities
KR102444842B1 (en) Apparatus for producing ultra high purity electronics grade carbondioxide
US5787730A (en) Thermal swing helium purifier and process

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 13815913

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 13815913

Country of ref document: EP

Kind code of ref document: A1