US3813889A - Separation of gas mixtures - Google Patents

Separation of gas mixtures Download PDF

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US3813889A
US3813889A US00126727A US12672771A US3813889A US 3813889 A US3813889 A US 3813889A US 00126727 A US00126727 A US 00126727A US 12672771 A US12672771 A US 12672771A US 3813889 A US3813889 A US 3813889A
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column
stream
liquid
methane
wash
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R Allam
B Bligh
L Gaumer
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Air Products and Chemicals Inc
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    • 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
    • F25J3/0204—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 characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • 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
    • B01D53/14—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 absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B23/00—Noble gases; Compounds thereof
    • C01B23/001—Purification or separation processes of noble gases
    • C01B23/0036—Physical processing only
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/506—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification at low temperatures
    • 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
    • F25J3/0204—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 characterised by the feed stream
    • F25J3/0223—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0252—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 characterised by the separated product stream separation of hydrogen
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0257—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 characterised by the separated product stream separation 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0261—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 characterised by the separated product stream separation of carbon monoxide
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/028—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 characterised by the separated product stream separation of noble gases
    • F25J3/029—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 characterised by the separated product stream separation of noble gases of helium
    • 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
    • F25J3/0295—Start-up or control of the process; Details of the apparatus used, e.g. sieve plates, packings
    • 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
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • 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
    • 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
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/08—Internal refrigeration by flash gas recovery loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/24—Quasi-closed internal or closed external carbon monoxide refrigeration cycle
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/42—Modularity, pre-fabrication of modules, assembling and erection, horizontal layout, i.e. plot plan, and vertical arrangement of parts of the cryogenic unit, e.g. of the cold box
    • 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
    • Y02C20/20—Capture or disposal of greenhouse gases of methane
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/92—Carbon monoxide
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/931—Recovery of hydrogen
    • Y10S62/933—From helium

Definitions

  • Hydrogen and/or helium is taken 2,545,778 3/1951 Haringhuizen 62/22 from the top of the column; a liquid stream containing 2,596,785 4/l952 Nelly 62/28 methane and nitrogen and/or carbon monoxide is 2,690,060 9/1954 Legatski 62/28 taken f the bottom; 2,933,901 4/1960 Davison 62/17 3,021,682 2/1962 Baker 62/39 7 Claims, 6 Drawing Figures M ENTED 4
  • This invention relates to the separation of gases, in particular, mixtures containing hydrogen and carbon monoxide.
  • a process in which a gas mixture containing hydrogen, and at least one of nitrogen and carbon monoxide is fed into the bottom of a column containing sieve trays, or other liquid vapour contacting devices, and liquid methane is fed into the top of the column.
  • the liquid methane absorbs the greater part of the nitrogen and/or carbon monoxide, and a product of fairly pure hydrogen is obtained from the top of this column. If the feed gas is less than 90 molar percent hydrogen, a substantial amount of heat is given up when the nitrogen and/or carbon monoxide is transferred from the gas phase to the liquid phase: this heat is herein called the heat of absorption.
  • a further object of this invention is to give a product of substantially pure carbon monoxide or substantially pure nitrogen.
  • a process in which a gas mixture including at least one of hydrogen and helium, and at least one of nitrogen and carbon monoxide, being at a pressure in the range atmospheres to 55 atmospheres, is cooled near to its dew point and is fed into the bottom ofa wash-column, into which liquid methane is fed at the top;
  • the washcolumn contains provision for bringing a refrigeration stream into indirect contact with the aforesaid gas mixture and the liquid methane;
  • a gas stream is taken from the top of the wash-column consisting of hydrogen and- /or helium substantially free from nitrogen and carbon monoxide, and a liquid stream is taken from the bottom of the wash-column containing methane and at least one of nitrogen and carbon monoxide.
  • the liquid taken from the bottom of the washcolumn, containing methane together with nitrogen and/or carbon monoxide and a small quantity of dissolved hydrogen, can be reduced in pressure in one or more stages, and the hydrogen rich flash gas removed as a waste stream, which can be recycled to the feed if required.
  • the liquid can then be distilled to obtain a stream of substantially pure liquid methane, and a stream of carbon monoxide and/or nitrogen substantially free of methane and hydrogen.
  • the stream of substantially pure liquid methane is pumped to a pressure sufficientto enable it to be fed into the top of the washcolumn.
  • the process requires a make-up of methane to replace losses in the gaseous product streams.
  • This can be methane in the feed gas stream, or methane from some outside source.
  • the invention further provides wash-column apparatus receiving at the bottom a gas mixture containing at least one of hydrogen and helium and at least one of nitrogen and carbon monoxide, said gas mixture being at a pressure in the range 5 atmospheres to 55 atmospheres, and receiving at the top a feed of liquid methane, the column having means for refrigeration of the vapour and liquid flows therein comprising one or more vapour/liquid contactors and a plurality of cooling coils.
  • FIG. 1 is a diagrammatic elevation of the washcolumn
  • FIG. 2 shows a single plate of the column in plan
  • FIG. 3 shows two consecutive plates in elevation
  • FIG. 4 is a flow sheet of a complete plant incorporating the wash-column
  • FIGS. 5A and 58 form a flow sheet of an alternative plant.
  • FIGS. 1, 2 and 3 The preferred design of the wash column is shown in FIGS. 1, 2 and 3. It is a counter-current vapour/liquid contacting device having means for providing heat exchange between the vapour/liquid mixture present and a boiling refrigerant.
  • the device can be considered as two sections.
  • the top section of the wash-column I contains a number of horizontal perforated plates 2 fitted with side downcomers 3, inlet weirs 4 and outlet weirs 5. Liquid flowing down the wash column passes across the plates in a side-to-side manner as in a conventional distillation column.
  • a number of tubes 6, each coiled in a flat spirally-wound coil are placed one above the other on the perforated area of the tray. The number of coiled tubes is such that the tube surfaces will be immersed in the biphase mixture which exists above the sieve tray perforations.
  • the spacing between the coils in a vertical direction, and between the bottom coil and the tray is sufficient to allow liquid to flow across the tray, while the distance horizontally between the tubes within a coil is sufficient to allow the vapour to pass vertically upwards through the coils.
  • the perforations on the tray are confined to an area vertically below the coils and bounded by the outside and inside coil perimeters.
  • inwardlydirected barriers 7 are placed at the edge of the column between the inlet and outlet weirs 4 and 5.
  • perforated area and downcomers are possible, and depending on the shape of the perforated area, flat coils of other than an oval shape may be required.
  • Liquid refrigerant passes down pipe 8 from a reservoir 10 and the vapour, together with any excess liquid, returns to the reservoir 10 through pipe 9.
  • the reservoir 10 acts as a vapour/liquid separator for the fluid returning along pipe 9.
  • valves 11 which isolate the coils on different groups of trays. These valves are used to adjust the refrigerant flowrate to each of the tray groups so that the correct temperature profile can be maintained across the column to give the optimum mass transfer between the gas and liquid phases.
  • the bottom section of the wash-column comprises a number of co-current vapour liquid contactors 12 in which there is provision for heat exchange with the refrigerant stream. They are constructed in this example on the well-known aluminum plate-fin matrix principle. Liquid refrigerant enters the contactors through pipe 8 via valves 13, which allow the refrigerant flow to be adjusted to maintain the correct temperature profile across the column. The refrigerant vapour, together with any excess liquid, leaves the contactors along pipes 14, which join into the common return header 9. For each contactor, liquid from the stage above flows in along pipe while vapour from the stage beneath flows in along pipe 16. The feed to the column enters the bottom contactor via pipe 17.
  • vapour and liquid feeds which have entered the contactor are mixed together evenly within the contactor and flow upwards through a common set of passages, which are adjacent to the refrigerant passage.
  • the length of the passages and the fluid velocities are such as to ensure that the liquid vapour mixture has substantially reached equilibrium, and that the required amount of heat transfer has taken place when the vapour liquid stream leaves the contactor.
  • the liquid-vapour mixture leaving each contactor along pipe 18 enters a vapour liquid separator 19.
  • the separators are arranged in a vertical column which is a continuation of the shell of the upper section of the wash-column, the contactors 12 being external to this.
  • vapour-liquid contactor heat exchangers l2 is necessary when the amount of heat transfer required per equilibrium stage in the column exceeds that which can be accomplished on one or two of the sieve trays using the flat coils.
  • the relative position of contactors and separators or sieve trays within the wash-column depends on the characteristics of the mixture which is to be separated.
  • the liquid methane enters the top of the column along pipe 20.
  • the gaseous product leaves the top of the column along pipe 21 while the liquid bottom product leaves the column along'pipe 22.
  • FIG. 4 being a flow sheet of the first.
  • the feed gas from which carbon dioxide and water have been removed, having a com position given in Table l, enters the multipass plate-fin heat exchanger 23 along pipe 24 at a pressure of 161 psia and a temperature of 48F, and is cooled to 270F.
  • lt passes from the heat exchanger to the washcolumn along pipe 17.
  • the wash liquid consisting of 99 percent methane enters the column at -292F along pipe 20. This wash liquid absorbs most of the carbon monoxide and nitrogen in the feed gas and the resulting hydrogen product having a composition given in Table 1 leaves the top of the column through pipe 21; passes through the multipass heat exchanger 23 and leaves the plant at 154 psia and 58F along pipe 25.
  • the heat of absorption in the wash column is removed by a boiling carbon monoxide stream which flows to the column along pipe 8 and returns as a vapour-liquid mixture along pipe 9 to the reservoir 10.
  • the liquid leaving the bottom of the wash-column along pipe 22 is flashed to 70 psia and passes into a separator 26.
  • the separator contains a heating coil 27 through which liquid methane is circulated to vaporize a small portion of the liquid and reduce the amount of hydrogen which remains dissolved in the liquid.
  • the vapour leaving separator 26 along pipe 56 passes through the multipass heat exchanger 23 and leaves the plant as waste gas along pipe 28.
  • the liquid leaves separator 26 through pipe 29, is
  • This column separates the fluid into a substantially pure carbon monoxide stream, having the composition given in Table l, which leaves the top of the column through pipe 32, and a liquid methane stream which leaves the bottom of the column through pipe 33, is raised in pressure to 165 psia in pump 34, passes through the heating coil 27 and enters the wash-column through line 20 after having been cooled in heat exchanger 30 to 292F.
  • a small quantity ofliquid methane is passed along pipe 35, reduced in pressure to 70 psia, heated in the multipass heat exchanger 23 to 58F, and leaves the plant in the waste gas through pipe 28.
  • the plant refrigeration, together with the washcolumn refrigeration, and the reflux and reboil to column 31, is provided by a circulating carbon monoxide stream.
  • Low pressure carbon monoxide gas leaving column 31 through line 32 and separator 10 through line 36 passes through the multipass heat exchanger 23 where it is heated to 58F before entering the first stage of the compressor 37.
  • the carbon monoxide stream is compressed in the first stage from 36 psia to 131 psia.
  • the product carbon monoxide stream leaves the plant along pipe 38 while a stream of gaseous carbon monoxide enters the multipass heat exchanger along pipe 39.
  • the remaining carbon monoxide gas enters the second stage of the compressor 37 and is compressed to 394 psia and enters the multipass heat exchanger 23 along pipe 40.
  • a high pressure gaseous carbon monoxide stream leaves the multipass heat exchanger 23 at a temperature of-l F through pipe 41 and enters the turbo-expander 42 where it is expanded to 129 psia and a temperature of 255F and leaves through pipe 43.
  • the remaining high pressure carbon monoxide stream leaves the multipass heat exchanger along pipe 44 at 2 l 6F and condenses in the reboiler-condenser 45, providing the heat duty to boil the liquid methane stream which is taken from the base of the column 31 through pipe 46 and returned as vapour through pipe 47.
  • the liquid carbon monoxide stream leaving reboilercondenser 45 along pipe 48 enters the multipass heat exchanger 23 at a temperature of 232F and is cooled down to 270F leaving through pipe 49.
  • Part of stream 49 is expanded down to 41 psia and introduced into the top of column 31 as reflux through pipe 50; the remainder of the high pressure liquid carbon monoxide stream is let down to 42 psia at valve 51 and is passed through the cold end of heat exchanger 30 where it cools the liquid methane wash liquid and it is then fed into the liquid carbon monoxide reservoir 10 through pipe 52.
  • the gaseous carbon monoxide stream at 131 psia entering the warm end of the multipass heat exchanger 23 along pipe 39 is cooled to 270F and leaves the cold end through pipe 53 where it joins the turbo-expander exhaust stream 43.
  • the wash column is divided into three sections. The bottom two sections 11 and 19 which are The third section 59 consists of distillation trays hav uid removes the last traces of carbon monoxide in the 'streams' pass through pipe 54 to the heat exchanger 30 where they are condensed.
  • the liquid carbon monoxide stream at 128 psia leaving heat exchanger 30 through pipe 55 is reduced in pressure to 41 psia and fed into the liquid carbon monoxide reservoir 10.
  • the waste gas stream 56 and the waste methane stream 35 can be taken through separate passages in the multipass heat exchanger 23, and the waste gas can then'be recycled to the feed stream 24after being compressed from 65 psia to 161 psia. This will result in an increase in the recovery of carbon monoxide.
  • the liquid stream leaving separator 26 through line 29 can be passed into a separator after being reduced in pressure to 42 psia and a hydrogen rich waste gas stream can be removed. This will result in the hydrogen concentration of the product carbon monoxide stream being reduced from0.0049 mole fraction to 0.0005 mole fraction.
  • the expander flow can be taken from the 131 psia intermediate pressure carbon monoxide stream, and the expander exhaust can discharge at 41 psia into the low pressure carbon I monoxide stream.
  • the second plant to be described, with reference to FIGS. 5A and 5B, is designed to produce hydrogen containing less than ppm of total impurities.
  • the feed gas from which carbon dioxide and water have been removed having the composition given in Table 2, is mixed with a recycle gas stream flowing through pipe 57 from compressor 58, and the mixture enters the multipass plate-fin heat exchanger 23 along pipe 24 at a pressure of 161 psia and a temperature of 50F. It is cooled to 270F and passes from the multipass plate-fin heat exchanger to the wash column cooled by boiling carbon monoxide refrigerant, are shown in FIGS. 1 to 3 and described above.
  • the liquid carbon monoxide flows to the column along pipe 8 and returns as a vapour-liquid mixture to the reservoir 10 along pipe 9.
  • hydrogen leaving the propane scrub column pipe 62 has a composition given in Table 2.
  • ltthen flows through one of the beds of a dual bed carbon adsorber 63 where the remaining nitrogen and methane are removed.
  • the adsorber vessels are switched over at regular intervals and heated up to 250F by means of a dry reactivation gas which enters along pipe 64 and leaves along pipe 65.
  • the hydrogen product gas having a composition given in Table 2 leaves the adsorbers along pipe 66, passes through the multipass plate-fin heat exchanger 23, and leaves the plant at 154 psia and 58F along pipe 25.
  • the propane containing methane leaves the bottom of the propane wash column along pipe 67 and is then reduced in pressure to psia and heated to 178F in heat exchanger 68 before being introduced into the propane stripping vessel 69.
  • the propane is stripped of methane in a single stage vapourliquid contact with hydrogen gas which is taken from stream 25 and reduced in pressure to 100 psia, and introduced directly into vessel 69 along pipe 70.
  • the temperature in the stripping vessel 69 is -l40F.
  • the purified propane leaving the bottom of vessel 69 along pipe'7 l is mixed with a small amount of propane makeup from pipe 72 to compensate for propane losses from the system.
  • the propane is cooled in heat exchanger 68 to 286F. and raised in pressure to psia in pump 73.
  • the liquid propane flows from the pump to heat exchanger 74 along pipe 75. It is cooled to 292F. by carbon monoxide which enters heat exchanger 74 along pipe'76 and returns to the liquid carbon monoxide reservoir 10 along pipe 77.
  • the liquid mixtureleaving the bottom of the wash 0 column along pipe 22 is flashed to 70 psia and passes into a separator 26.
  • the separator contains a heating coil 27 through which liquid methane is circulated to vaporise a small portion of the liquid mixture and reduce the amount of hydrogen which remains dissolved in the liquid mixture.
  • the wash liquid consisting of pure methane containing 5 ppm carbon monoxide enters the column at -292F along pipe 20.
  • the wash liqfeed gas in section 59 of the wash column and absorbs the bulk of the nitrogen and carbon monoxide in the feed gas in sections 1 and 19.
  • the hydrogen gas leaves the top of the column through pipe 21 and flows into an absorption column 60 fitted with vapour-liquid contacting devices such as sieve trays.
  • the hydrogen is scrubbed by a liquid propane stream which enters the column at a temperature of-292F along pipe 61.
  • the carbon monoxide recycle refrigeration system is identical to that described in the first plant example.
  • a process for removing impurities comprising at least one of the group of nitrogen and carbon monoxide from a gaseous feed stream having a principle compo nent comprising at least one of the group of hydrogen and helium comprising the steps of:
  • An absorption column comprising:
  • a. wall means forming a shell for the column
  • inlet means for introducing a gaseous feed stream connected to the lower portion of said column
  • inlet means for introducing a wash liquid connected to upper portion of said column
  • first and second outlet means for discharging a purified product stream and an impurity stream
  • partition means in the lower portion of said column forming a series of phase separators for separating said feed and wash fluids after direct contact thereof
  • a plurality of fluid contactors each of said contactors being connected to two of said phase separators for contacting gaseous feed and wash liquid from a phase separator thereabove,
  • a source of refrigerant connected to said fluid passage means in said contactors for passing refrigerant in indirect heat exchange with the feed and wash fluids for removing a substantial portion of the heat of absorption thereof.
  • the absorption column as claimed in claim 4 including a plurality of refrigeration coils positioned above at least some of said trays and immersed in the fluids on said trays for providing additional refrigeration to the top portion of said column.
  • the absorption column as claimed in claim 5 ineluding a source of refrigerant, a plurality of passage means connecting said plurality of refrigeration coils to v said source of refrigerant, and a plurality of valve means in said passage means for controlling the flowrate of refrigerant to said coils for maintaining an optimum temperature profile along the upper portion of QQRRECTEGN Patent No. 3,813,889 Dated June '4 19? Rodney John Allam, Bernard Ramsey Bligh & Lee S. Gaumer Inventor(s) It is certified that error appears in the above-identified patent and that said Letters Patent are hereby corrected as shown below:

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US4304634A (en) * 1972-11-17 1981-12-08 Southwest Services, Inc. Method for producing isotopically enriched helium-4 and use of same as nuclear reactor coolant
US4338107A (en) * 1980-10-30 1982-07-06 Union Carbide Corporation Wash system gas separation
EP0092770A3 (en) * 1982-04-28 1985-03-20 Linde Aktiengesellschaft Process for obtaining carbon monoxide
US4838913A (en) * 1988-02-10 1989-06-13 Union Carbide Corporation Double column air separation process with hybrid upper column
US5282365A (en) * 1992-11-17 1994-02-01 Praxair Technology, Inc. Packed column distillation system
US5329775A (en) * 1992-12-04 1994-07-19 Praxair Technology, Inc. Cryogenic helium production system
US5351491A (en) * 1992-03-31 1994-10-04 Linde Aktiengesellschaft Process for obtaining high-purity hydrogen and high-purity carbon monoxide
US5490391A (en) * 1994-08-25 1996-02-13 The Boc Group, Inc. Method and apparatus for producing oxygen
US6082134A (en) * 1997-07-29 2000-07-04 Air Products And Chemicals, Inc. Process and apparatus for separating a gaseous mixture
US6094938A (en) * 1998-04-09 2000-08-01 Air Products And Chemicals, Inc. Separation of carbon monoxide from gaseous mixtures containing carbon monoxide and hydrogen
US20020129622A1 (en) * 2001-03-15 2002-09-19 American Air Liquide, Inc. Heat transfer fluids and methods of making and using same
US6578377B1 (en) * 2002-03-11 2003-06-17 Air Products And Chemicals, Inc. Recovery of hydrogen and carbon monoxide from mixtures including methane and hydrocarbons heavier than methane
US6651358B2 (en) * 2001-04-30 2003-11-25 American Air Liquide, Inc. Heat transfer fluids and methods of making and using same comprising hydrogen, helium and combinations thereof
EP1479989A1 (en) * 2003-05-19 2004-11-24 L'Air Liquide S. A. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Process and installation for providing gaseous carbon monoxide and/or a mixture containing carbon monoxide
US20050047995A1 (en) * 2003-08-29 2005-03-03 Roger Wylie Recovery of hydrogen from refinery and petrochemical light ends streams
FR2910603A1 (fr) * 2006-12-21 2008-06-27 Air Liquide Procede de separation d'un melange de monoxyde de carbone, de methane, d'hydrogene et eventuellement d'azote par distillation cryogenetique
FR2916264A1 (fr) * 2006-12-21 2008-11-21 Air Liquide Procede de separation d'un melange de monoxyde de carbone, de methane, d'hydrogene et eventuellement d'azote par distillation cryogenique
WO2008052776A3 (de) * 2006-11-02 2008-12-31 Linde Ag Verfahren und vorrichtung zur zerlegung von synthesegas mittels methanwäsche
US20100135892A1 (en) * 2009-05-06 2010-06-03 Bahr David A Absorption method for recovering gas contaminants at high purity
EP2226598A2 (en) 2009-03-03 2010-09-08 Air Products and Chemicals, Inc. Separation of carbon monoxide from gaseous mixtures containing carbon monoxide
WO2025068532A1 (en) * 2023-09-29 2025-04-03 Yara International Asa Sieve tray for absorber

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DE3149846A1 (de) * 1981-12-16 1983-07-21 Linde Ag, 6200 Wiesbaden "verfahren und vorrichtung zur zerlegung von syntheseabgas"
FR2807504B1 (fr) * 2000-04-07 2002-06-14 Air Liquide Colonne pour separation cryogenique de melanges gazeux et procede de separation cryogenique d'un melange contenant de l'hydrogene et du co utilisant cette colonne

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Cited By (30)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4304634A (en) * 1972-11-17 1981-12-08 Southwest Services, Inc. Method for producing isotopically enriched helium-4 and use of same as nuclear reactor coolant
US4338107A (en) * 1980-10-30 1982-07-06 Union Carbide Corporation Wash system gas separation
EP0092770A3 (en) * 1982-04-28 1985-03-20 Linde Aktiengesellschaft Process for obtaining carbon monoxide
US4838913A (en) * 1988-02-10 1989-06-13 Union Carbide Corporation Double column air separation process with hybrid upper column
US5351491A (en) * 1992-03-31 1994-10-04 Linde Aktiengesellschaft Process for obtaining high-purity hydrogen and high-purity carbon monoxide
US5282365A (en) * 1992-11-17 1994-02-01 Praxair Technology, Inc. Packed column distillation system
US5329775A (en) * 1992-12-04 1994-07-19 Praxair Technology, Inc. Cryogenic helium production system
US5490391A (en) * 1994-08-25 1996-02-13 The Boc Group, Inc. Method and apparatus for producing oxygen
US6082134A (en) * 1997-07-29 2000-07-04 Air Products And Chemicals, Inc. Process and apparatus for separating a gaseous mixture
US6094938A (en) * 1998-04-09 2000-08-01 Air Products And Chemicals, Inc. Separation of carbon monoxide from gaseous mixtures containing carbon monoxide and hydrogen
US20020129622A1 (en) * 2001-03-15 2002-09-19 American Air Liquide, Inc. Heat transfer fluids and methods of making and using same
US6651358B2 (en) * 2001-04-30 2003-11-25 American Air Liquide, Inc. Heat transfer fluids and methods of making and using same comprising hydrogen, helium and combinations thereof
US6578377B1 (en) * 2002-03-11 2003-06-17 Air Products And Chemicals, Inc. Recovery of hydrogen and carbon monoxide from mixtures including methane and hydrocarbons heavier than methane
WO2004102094A1 (en) * 2003-05-19 2004-11-25 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for supplying gaseous carbon monoxide and/or a gaseous mixture containing at least 10% carbon monoxide
US20060254311A1 (en) * 2003-05-19 2006-11-16 Jean Billy Process and installation for supplying gaseous carbon monoxide and/or a gaseous mixture containing at least 10% carbon monoxide
EP1479989A1 (en) * 2003-05-19 2004-11-24 L'Air Liquide S. A. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude Process and installation for providing gaseous carbon monoxide and/or a mixture containing carbon monoxide
US20050047995A1 (en) * 2003-08-29 2005-03-03 Roger Wylie Recovery of hydrogen from refinery and petrochemical light ends streams
US7036337B2 (en) * 2003-08-29 2006-05-02 Wylie Companies, Inc Recovery of hydrogen from refinery and petrochemical light ends streams
WO2008052776A3 (de) * 2006-11-02 2008-12-31 Linde Ag Verfahren und vorrichtung zur zerlegung von synthesegas mittels methanwäsche
US20100043489A1 (en) * 2006-12-21 2010-02-25 Arthur Darde Method For Separating A Mixture Of Carbon Monoxide, Methane, Hydrogen And Optionally Nitrogen by Cryogenic Distillation
FR2916264A1 (fr) * 2006-12-21 2008-11-21 Air Liquide Procede de separation d'un melange de monoxyde de carbone, de methane, d'hydrogene et eventuellement d'azote par distillation cryogenique
WO2008087318A3 (fr) * 2006-12-21 2009-11-26 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé de séparation d'un mélange de monoxyde de carbone, de méthane, d'hydrogène et éventuellement d'azote par distillation cryogénique
FR2910603A1 (fr) * 2006-12-21 2008-06-27 Air Liquide Procede de separation d'un melange de monoxyde de carbone, de methane, d'hydrogene et eventuellement d'azote par distillation cryogenetique
CN101680713B (zh) * 2006-12-21 2013-08-14 乔治洛德方法研究和开发液化空气有限公司 通过低温蒸馏分离包含一氧化碳、甲烷、氢和可选的氮的混合物的方法
US8959952B2 (en) * 2006-12-21 2015-02-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for separating a mixture of carbon monoxide, methane, hydrogen and optionally nitrogen by cryogenic distillation
EP2226598A2 (en) 2009-03-03 2010-09-08 Air Products and Chemicals, Inc. Separation of carbon monoxide from gaseous mixtures containing carbon monoxide
US20100223952A1 (en) * 2009-03-03 2010-09-09 Air Products And Chemicals, Inc. Separation of Carbon Monoxide From Gaseous Mixtures Containing Carbon Monoxide
US8640495B2 (en) 2009-03-03 2014-02-04 Ait Products and Chemicals, Inc. Separation of carbon monoxide from gaseous mixtures containing carbon monoxide
US20100135892A1 (en) * 2009-05-06 2010-06-03 Bahr David A Absorption method for recovering gas contaminants at high purity
WO2025068532A1 (en) * 2023-09-29 2025-04-03 Yara International Asa Sieve tray for absorber

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FR2083590A1 (Direct) 1971-12-17
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DE2116326A1 (de) 1972-09-07

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