WO2009155454A2 - Procédé de séparation d'air hybride à enrichissement préliminaire non cryogénique et purification cryogénique faisant appel à un générateur de gaz ou de liquide à un seul composant - Google Patents

Procédé de séparation d'air hybride à enrichissement préliminaire non cryogénique et purification cryogénique faisant appel à un générateur de gaz ou de liquide à un seul composant Download PDF

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Publication number
WO2009155454A2
WO2009155454A2 PCT/US2009/047850 US2009047850W WO2009155454A2 WO 2009155454 A2 WO2009155454 A2 WO 2009155454A2 US 2009047850 W US2009047850 W US 2009047850W WO 2009155454 A2 WO2009155454 A2 WO 2009155454A2
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air
oxygen
nitrogen
high purity
heat exchanger
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WO2009155454A3 (fr
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William Brigham
Nick Ortenberg
Michael Schroeder
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Priority to US12/999,965 priority Critical patent/US20110100055A1/en
Priority to CA2728244A priority patent/CA2728244A1/fr
Publication of WO2009155454A2 publication Critical patent/WO2009155454A2/fr
Publication of WO2009155454A3 publication Critical patent/WO2009155454A3/fr
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • C01B13/0251—Physical processing only by making use of membranes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • C01B13/0259—Physical processing only by adsorption on solids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • C01B13/0259—Physical processing only by adsorption on solids
    • C01B13/0277—Temperature swing adsorption
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04163—Hot end purification of the feed air
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/044—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a single pressure main column system only
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04636—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a hybrid air separation unit, e.g. combined process by cryogenic separation and non-cryogenic separation techniques
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/10—Nitrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/12—Oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/10—Single element gases other than halogens
    • B01D2257/102—Nitrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
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    • B01D2257/10—Single element gases other than halogens
    • B01D2257/104—Oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D2257/00—Components to be removed
    • B01D2257/80—Water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/416—Further details for adsorption processes and devices involving cryogenic temperature treatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0462—Temperature swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0043—Impurity removed
    • C01B2210/0046—Nitrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0043—Impurity removed
    • C01B2210/0051—Carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes 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
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/80—Processes or apparatus using other separation and/or other processing means using membrane, i.e. including a permeation step
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
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    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the invention relates to the field of air separation plants, nitrogen or oxygen generators and high pressure nitrogen or oxygen delivery systems, including (but not limited to) those used for drilling and servicing oil and gas we Hs.
  • non-cryogenic gas generators are often used, in these generators, gas is made at the point of use by supplying compressed air to a pressure/vacuum and/or temperature swing adsorption (i.e. PSA/VSA/TSA) system or to a permeable membrane system.
  • Nitrogen is typically made available at 95% purity as determined by a measurement of less than 5% oxygen; oxygen is typically made available at 93% purity.
  • This approach is widely used to address the logistical issues involved with using liquid, but the pressures achievable (less than 5000 psig) are limited by the existing gas compression equipment, and purities are limited to no more than 99% for nitrogen and 93% for oxygen.
  • these non-cryogenic systems can only deliver at best approximately 50% and typically 35% to 45% of the available desired component in the feed flow as a product; the remaining is eliminated as a waste gas.
  • Another method for supplying nitrogen gas on ⁇ site is to use a cryogenic gas plant.
  • This system uses the cryogenic distillation process to make high purity nitrogen, which it delivers as a Sow pressure gas.
  • the low pressure nitrogen gas then needs to be boosted up to a workable pressure, and the available boosters limit the pressure to around 5000 psig.
  • the height of the distillation equipment required by this process is, by necessity, usually very tall (35 to 40 ft or taller) and difficult to transport and set up.
  • the illustrated general embodiment of the invention is an air separation plant for generating either high purity nitrogen or oxygen (depending on the internals of the separation and distillation modules) comprising a compressor, cleansing module, initial non-cryogenic separation module, and a cryogensc distillation module,
  • the cleansing module serves to prepare the compressed air for the enrichment process.
  • the air flow is thoroughly cleaned, mechanical impurities and free wafer are taken out, and then the air is thermaiiy conditioned to have the temperature optima! to the enrichment process (i.e. 130 0 F for the permeable membrane array),
  • the non-cryogenic separation module serves to enrich the process flow with desired component (final product of the separation) and to strip it from all other undesirable elements (mainly water vapor and carbon dioxide).
  • the distillation module serves to finalize the separation and make the final product. If the final product should be delivered as high pressure gas, then internally, within the distillation module, the product is pressurized as a liquid, an ⁇ only then is evaporated in the main heat exchanger. [015] Enriching of the feed flow to the distillation module with the desired component (oxygen for oxygen generators and nitrogen for nitrogen generators) requires fewer trays inside the distillation column than would be required if non- enriched air would have been supplied to the distillation column.
  • the illustrated embodiment also comprises a method of generating high purity one component gas from the air by processing the compressed air in three stages: (1) cleansing the compressed air from free water and mechanical impurities, (2) enriching it with a desired component by one of the non-cryogenic methods known (physical, chemical or physical-chemical) and finally (3) finalizing separation by using a cryogenic fractional distillation module.
  • Fig. 1 is a block diagram of the hybrid cryogenic gas generator with non-cryogenic assist of the iliustrated general embodiment.
  • Fig. 2 is a schematic diagram of the hybrid cryogenic low pressure nitrogen gas generator with non-cryogenic assist of the illustrated genera! embodiment shown in Fig, 1 ,
  • FIG. 3 is a schematic diagram of the hybrid cryogenic high pressure nitrogen gas generator with non-cryogenic assist of the illustrated genera! embodiment shown in Fig.1.
  • Fig, 4 is a schematic diagram of the hybrid cryogenic liquid nitrogen generator with non-cryogenic assist of the illustrated general embodiment shown in Fig.1.
  • FIG. 5 is a schematic diagram of the hybrid cryogenic low pressure oxygen gas generator with non-cryogenic assist of the illustrated general embodiment shown in Fig.1 ,
  • Fig. 6 is a schematic diagram of the hybrid cryogenic high pressure oxygen gas generator with non-cryogenic assist of the iliustrated general embodiment shown in Fig.1.
  • Fig. 7 is a schematic diagram of the hybrid cryogenic liquid oxygen generator with non-cryogenic assist of the illustrated genera! embodiment shown in Fig. 1.
  • the illustrated genera! embodiment of the invention shown in Fig.1 is a method for producing and delivering high purify single component gas such as nitrogen or oxygen at high pressures of up to 15,000 ps ⁇ g using an apparatus with a significantly lower profile of no more than 20 feet of overaii height than would otherwise be required.
  • a conventional cryogenic gas plant distillation unit (a.k.a. cold box) is supplemented at the front end by using a separation module with a non-cryogenic enrichment system not oniy to clean the air of water and carbon dioxide, as is normally required by the cryogenic distillation cycle, but additionally, to significantly enrich the feed flow with the desired component by removing a significant amount of the undesired component.
  • the removal of the undesired component before the cryogenic process located in the distillation module permits the distillation column to be significantly shorter than otherwise would be required. This in turn reduces the height of the equipment such that it can easily be transported and setup.
  • the current invention comprises six main embodiments, namely a method and apparatus for producing low pressure nitrogen gas, high pressure nitrogen gas, liquid nitrogen, low pressure oxygen gas, high pressure oxygen gas, and liquid oxygen.
  • One of the preferred embodiments of the invention shown in Fig.2 is a method and apparatus that combines two technologies into a hybrid system that can deliver high purity nitrogen gas while increasing the portability, compact size, and operational convenience of an on-site non-cryogenic generator.
  • Another one of the preferred embodiments of the invention as shown in Fig. 3 is a method and apparatus that combines three technologies into a hybrid system that can deliver high purity nitrogen gas at high pressures that are typically only achievable by pumping liquid nitrogen from delivered liquid, while increasing the portability, compact size, and operational convenience of an on-site non-cryogenic generator.
  • FIG. 5 In still another one of the preferred embodiments of the invention as shown in Fig. 5 is a method and apparatus that combines two technologies into a hybrid system that can deliver high purity oxygen gas while improving the portability, compact size, and operational convenience of an on-site non- cryogenic generator.
  • FIG. 6 In yet another one of the preferred embodiments of the invention as shown in Fig. 6 is a method and apparatus that combines three technologies into a hybrid system that can deliver high purity oxygen gas at high pressures that are typically only achievable by pumping liquid oxygen from delivered liquid while improving the portability, compact size, and operational convenience of an on-site non-cryogenic generator.
  • Fig. 7 is a method and apparatus that combines two technoiogies into a hybrid system that can deliver high purity liquid oxygen that is available through the cryogenic process while improving the portability, compact size, and operational convenience of an on-site non-cryogenic generator which cannot produce liquid.
  • All the illustrated embodiments of the invention depicted in Figs.2-7 include a diesel or electric d ⁇ ve or engine 1 that drives an air compressor 2, which pressurizes the air to 200 to 500 psig.
  • the pressurized air is then passed through a cleansing module 3, which comprises of at least an air-to-air heat exchanger 31 , where it is cooled to near ambient temperatures;
  • A a centrifugal separator 32 to remove free water;
  • a particulate filter 33 that removes particles and condensates down typically down to 3 microns;
  • a coalescing filter 34 which removes any remaining fine oil vapor and further condensates from the air, typically down to 0.5 microns or less; an activated carbon bed 35 which removes any remaining hydrocarbons and other contaminants; and a reheater 37 for the purpose of insuring that the moisture remaining in the stiil saturated air remains in the vapor stage and does not condense on the piping or in any other component of the apparatus.
  • the cleaned and prepared compressed air is then directed to a separation module 4 comprising a temperature swing absorption system (TSA) 1 a pressure swing absorption system (PSA) 1 a vacuum swing absorption system (VSA), a permeable membrane array, or a combination of aforementioned technologies which is tuned or arranged and configured to remove all remaining water and carbon dioxide from the cleaned air, typica ⁇ y to less than 5 ppm water and less than 15 ppm carbon dioxide.
  • TSA temperature swing absorption system
  • PSA pressure swing absorption system
  • VSA vacuum swing absorption system
  • permeable membrane array or a combination of aforementioned technologies which is tuned or arranged and configured to remove all remaining water and carbon dioxide from the cleaned air, typica ⁇ y to less than 5 ppm water and less than 15 ppm carbon dioxide.
  • the undesired component is also partially removed as a waste gas although the separation module 4 is not optimized for removal of the undesired component.
  • the separation module 4 is better used for enrichment of the flow with the desired component
  • the cleaned enriched air is fed to cold box 5, which comprises a heat exchanger 51 , where the enriched air is cooied by the exiting waste gas and the high purity product, the enriched air is then expanded in the turbo expander 52.
  • the enriched air from the turbo-expander 52 is then delivered to a distillation column 53 where final separation to the desired purity of the nitrogen is achieved and to a evaporator-reboiler 55.
  • the evaporator-reboilar 55 is used to liquefy the gaseous nitrogen which then irrigates the distillation column 53 .
  • the enriched air from the turbo-expander 52 is then delivered to the bottom of the evaporator-reboiler 55 where it is liquefied. The liquid air is then throttled into the top of the distillation column 53 for final separation.
  • Liquid oxygen collects in the top of evaporator-reboiler 55 where some evaporates to generate a gas flow up through distillation column 53.
  • waste gas from the top of the evaporator-reboiler 55, or in the corresponding oxygen system embodiments of Figs. 5-7, waste gas from the top of the distillation column 53 is sent back to the heat exchanger 51 where if is heated by absorbing heat from the incoming enriched feed air as disclosed above and is then released to the atmosphere,
  • the product from the distillation column 53 is forwarded to the heat exchanger 51 in a separate passage than the waste gas where it is heated by absorbing heat from the enriched feed air as disclosed above and is then forwarded to the final application,
  • the liquid product is pressurized to the desired level by a cryogenic pump 56 which is integral to the cold box 5.
  • the high pressure liquid then goes to a high pressure version of heat exchanger 51 for vaporization and cooling of the incoming enriched feed air.
  • the high pressure gas that is produced is then forwarded to the final application.
  • the purified product can be taken from the distillation column 53, bypassing the heat exchanger 51 and forwarded to the customer for usage or storage.
  • This smaller heat exchanger 51 and distillation column 53 make the overall system much smaller and easier to transport and setup as compared to a conventional cryogenic gas plant
  • the entire system 10 can be installed in a conventional 20 foot shipping container, laying distillation column 53 lengthwise in the container, and then upending the container for operation.
  • Another aspect of the present invention is the capability of delivering very high pressures, such as are typically only achieved in a liquid nitrogen or liquid oxygen pumping system.
  • a standard cryogenic gas plant design takes the low pressure liquid nitrogen or oxygen that comes off the distillation column and passes it through a heat exchanger counter-flow with the incoming air. This serves to warm the newly generated nitrogen or oxygen and starts to coo! the incoming air, recovering a significant portion of the refrigeration.
  • the present invention places a high pressure liquid pump 56 in the circuit before the last pass through the heat exchanger 51 in Figs. 3 and 6.
  • This pump 56 raises the pressure of the liquid as high as 10,000 to 15,000 psig.
  • Such high pressures are not achievable in a conventional on-site PSA or membrane based nitrogen or oxygen generation system.
  • the high pressure liquid is then vaporized in the special high pressure version of heat exchanger 51 designed for this purpose.
  • the illustrated embodiment of the invention includes an apparatus for high purity extraction of a selected component from air comprising: a source of air; a cleaning module arranged coupled to the source of air and configured to preferentially remove carbon dioxide and water from the air; a non- cryogenic enrichment module coupled to the cleaning module to preferentially extract the selected component to produce a cleaned modified air mixture enriched in the selected component; and a liquefaction-distillation unit coupled to the enrichment module for liquefying the air mixture enriched in the selected component and separating the selected component from the modified air mixture to provide high purity liquid phase extraction of the selected component.
  • the liquefaction-distillation unit may thus comprise a shortened liquefaction-distillation column, which can be advantageous operated on a portable or moving platform, ship or vehicie.
  • the selected component is nitrogen or oxygen.
  • the illustrated embodiment includes a nitrogen plant for generating high purity nitrogen to an application comprising: a source of air including nitrogen and oxygen; a non-cryogenic separation module coupled to the source of air, the separation mod ⁇ ie arranged and configured to preferentially remove carbon dioxide and water from the air but also a portion of the oxygen; and a liquefaction-distillation unit coupled to the separation module for liquefying the nitrogen rich air produced by the non-cryogenic separation module and separating the oxygen from the nitrogen to produce high purity liquid nitrogen,
  • the plant further comprises a heat exchanger coupled to the liquefaction-distillation unit for vaporizing the high purity liquid nitrogen into a Sow pressure nitrogen gas.
  • the plant further comprises a pump coupled between the liquefaction-distillation unit and the heat exchanger for pressurizing the produced high purity liquid nitrogen wherein the heat exchanger is a high pressure heat exchanger , and wherein the liquid nitrogen output from the liquefaction- distillation unit is pumped at high pressure by the pump through the high pressure heat exchanger to deliver high pressure nitrogen gas from the high pressure heat exchanger.
  • the plant further comprises a multiple stage feed air preparation unit coupled between the source of air and the separation module to clean the air for delivery to the separation module.
  • the separation module in one embodiment is a molecular sieve type non-cryogenic gas separation system selected for its ability to remove water and carbon dioxide and oxygen from the air.
  • the separation module in another embodiment is a membrane array selected for its ability to remove water and carbon dioxide and oxygen from the air.
  • the illustrated embodiment of the invention also includes a method for high purify extraction of a selected component from air comprising the steps of preferentially removing carbon dioxide and water from air to provide cleaned
  • IO air, non-cryogenicalSy enriching the cleaned air in the selected component to provide an enriched modified air mixture, liquefying enriched modified air mixture, and fractionally distilling the liquefied modified air mixture to preferentially extract the selected component at high purity in liquid phase.
  • the fractional distillation may be performed in a shortened column or over a shorter vertical distance, which is an advantage when performed on a portable or moving platform, ship or vehicle.
  • the step of fractionally distilling the liquefied modified air mixture to preferentially extract the selected component at high purity in liquid phase comprises producing high purity liquid nitrogen or oxygen.
  • the illustrated embodiment of the invention thus also includes a method for generating high purity nitrogen to an application comprising the steps of providing a flow of air, removing carbon dioxide, water, and a portion of the oxygen from the compressed air to form a nitrogen rich gas, liquefying the nitrogen rich gas, and separating the remaining oxygen from the nitrogen rich liquid in a fractional distillation column to produce a high purity liquid nitrogen.
  • 056] The method further comprises vaporizing the high purity liquid nitrogen in a heat exchanger to produce a high purity Sow pressure nitrogen gas.
  • the method further comprises pressurizing of the high purity liquid nitrogen and vaporizing the high purity high pressure liquid nitrogen in a high pressure heat exchanger to produce a high purity high pressure nitrogen gas.
  • the method further comprises cleaning the air prior to removing carbon dioxide, water, and a portion of the oxygen from the flow of air.
  • the illustrated embodiment of the invention thus also includes an oxygen plant for generating high purity oxygen to an application comprising: a source of air including nitrogen and oxygen; a non-cryogenic separation module coupled to the source of air, the separation module arranged and configured to preferentially remove carbon dioxide and water from the air but also a portion of the nitrogen; a liquefaction-distillation unit coupled to the non-cryogenic separation module for liquefying the oxygen rich air produced by the non- cryogenic separation module and separating the nitrogen from the oxygen to produce high purity liquid oxygen.
  • the piant further comprises a heat exchanger coupled to the liquefaction-distillation unit for vaporizing the high purity liquid oxygen into a tow pressure oxygen gas.
  • the plant further comprises a pump coupled between the liquefaction-distillation unit and the heat exchanger for pressurizing the produced high purity liquid oxygen wherein the heat exchanger is a high pressure heat exchanger , and wherein the liquid oxygen output from the liquefaction-distillation unit is pumped to a high pressure by the pump through the high pressure heat exchanger to deliver high pressure oxygen gas from the high pressure heat exchanger.
  • the plant further comprises a multiple stage feed air preparation unit coupled between the source of air and the separation moduie to clean the air for delivery to the separation module .
  • the separation module in one embodiment is a molecular sieve type non-cryogenic gas separation system selected for its ability to remove water, carbon dioxide and nitrogen from the air.
  • the illustrated embodiment of the invention thus also includes a method for generating high purity oxygen to an appSication comprising the steps of providing a flow of air, removing carbon dioxide, water, and a portion of the nitrogen from the compressed air to form a oxygen rich gas, liquefying the oxygen rich gas, and separating the remaining nitrogen from the oxygen rich liquid in a fractional distillation column to produce a high purity liquid oxygen.
  • the method further comprises vaporizing the high purity liquid oxygen in a heat exchanger to produce a high purity low pressure oxygen gas.
  • the method further comprises pressurizing of the high purity liquid oxygen and vaporizing the high purity high pressure liquid oxygen in a high pressure heat exchanger to produce a high purify high pressure oxygen gas.
  • the method further comprises cleaning the air prior to removing carbon dioxide, water, and apportion of the nitrogen from the flow of air.

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Abstract

L'invention porte sur un système portable qui permet de produire de grandes quantités d'un gaz azote ou oxygène de grande pureté à haute pression. Selon l'invention, un système PSA, VSA, TSA ou à membrane perméable nettoie l'air en éliminant l'eau et le dioxyde de carbone, comme cela se fait normalement lors d'un cycle de distillation cryogénique, mais en élimine aussi une quantité significative d'oxygène ou d'azote, en fonction du gaz produit désiré. L'élimination de l'oxygène ou de l'azote préalablement au processus cryogénique permet d'utiliser une colonne de distillation significativement plus courte que d'ordinaire, entraînant une réduction de la taille de l'équipement qui rend ce dernier facile à transporter et à installer. On utilise en outre une pompe à liquide à haute pression pour augmenter la pression de l'azote ou de l'oxygène immédiatement avant leur admission dans l'échangeur de chaleur cryogénique où le liquide est vaporisé et le gaz entrant est refroidi.
PCT/US2009/047850 2008-06-19 2009-06-18 Procédé de séparation d'air hybride à enrichissement préliminaire non cryogénique et purification cryogénique faisant appel à un générateur de gaz ou de liquide à un seul composant Ceased WO2009155454A2 (fr)

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CA2728244A CA2728244A1 (fr) 2008-06-19 2009-06-18 Procede de separation d'air hybride a enrichissement preliminaire non cryogenique et purification cryogenique faisant appel a un generateur de gaz ou de liquide a un seul composant

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CN105911197B (zh) * 2016-05-25 2018-06-29 延边大学 全自动样品热解吸与液相微富集装置

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IT202000032657A1 (it) * 2020-12-29 2022-06-29 Saipem Spa Sistema di accumulo e produzione di energia per la stabilizzazione della rete elettrica
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CN105911197B (zh) * 2016-05-25 2018-06-29 延边大学 全自动样品热解吸与液相微富集装置

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