US3426543A - Combining pure liquid and vapor nitrogen streams from air separation for crude hydrogen gas washing - Google Patents

Combining pure liquid and vapor nitrogen streams from air separation for crude hydrogen gas washing Download PDF

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US3426543A
US3426543A US677839A US3426543DA US3426543A US 3426543 A US3426543 A US 3426543A US 677839 A US677839 A US 677839A US 3426543D A US3426543D A US 3426543DA US 3426543 A US3426543 A US 3426543A
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nitrogen
conduit
column
liquid
pure
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Rudolf Becker
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Linde GmbH
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Linde GmbH
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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
    • F25J3/0228—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
    • F25J3/0276—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 H2/N2 mixtures, i.e. of ammonia 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
    • F25J3/0204—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
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • 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
    • F25J3/04—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
    • 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work 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
    • 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
    • F25J3/04406—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 dual pressure main column system
    • F25J3/04412—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 dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • 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
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • F25J3/04587—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for the NH3 synthesis, e.g. for adjusting the H2/N2 ratio
    • 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
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04612—Heat exchange integration with process streams, e.g. from the air gas consuming unit
    • 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
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/12—Refinery or petrochemical off-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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/20—H2/N2 mixture, i.e. synthesis gas for or purge gas from ammonia synthesis
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
    • 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
    • Y10S62/934—From nitrogen

Definitions

  • An impure nitrogen stream from the high pressure column is recompressed and then cooled by vaporizing oxygen from the low pressure column as well as exiting ammonia synthesis gas and scrubber liquid streams from a crude hydrogen scrubber before returning to the high pressure column.
  • Separate streams of pure nitrogen liquid and vapor are removed from the high pressure column which streams are combined and completely liquefied with part of the liquid nitrogen being used to wash a crude hydrogen gas while another part of the pure liquefied nitrogen is added to the washed hydrogen to form a gas stream for ammonia synthesis.
  • This invention relates to a process for air fractionation and is particularly concerned with the use of a highly compressed gas in cold circulation for pressure vaporization of liquid oxygen, and with the use of a group of periodically transposable regenerators for heat exchange between the air to he fractionated and the oxygen.
  • the invention is also concerned with the separation of pure nitrogen, especially for the production of synthetic ammonia.
  • the invention is carried out in a very simple and economical manner by taking from the rectification column an impure fraction of circulating nitrogen, warming it to the temperature of the surroundings by passage through a regenerator which has been cleansed by scavenging with nitrogen during at least one preceding stage, liquefying the impure fraction by heat exchange after high compression and, preferably, after cleansing in an adsorber, and then, after passage through an expansion device, returning the impure nitrogen to the rectification column at a point near the place from which it was taken, whereby pure nitrogen is obtained from the head section of the column, preferably for independent use.
  • the impure nitrogen is preferably removed from the middle section of the pressure column and, after being at least partly liquefied, is returned to the same place.
  • the gas to be expanded can be taken, after sutfi-cient prewarming, from a suitable place on the regenerator through which circulating nitrogen is passed, and/ or if it bypasses this regenerator, is prewarmed by passage through a heat exchanger with circulating nitrogen before being returned to the pressure column.
  • the pure nitrogen is to be used for the synthesis of ammonia, it is advantageous to take the pure nitrogen from the head of the column in a partly liquid and partly gaseous state, in preferred proportions of 1 part liquid to 6-20 parts gas, the most preferred proportion being 1 part liquid to 10 par-ts gas; and after complete liquefaction with further cooling under the same pressure if necessary, it is subjected to heat exchange with possibly expanded products of a synthetic ammonia plant, is then compressed to the pressure of the washing column of that plant, and is used as a washing fluid for hydrogen gas and as a component of the ammonia synthesis gas. In this manner the necessity of compressing the gaseous nitrogen to the normally higher pressure of the washing column of the synthetic ammonia plant is avoided, and the pump for compressing the liquefied nitrogen uses much less energy.
  • the air to be fractionated enters by conduit 1, is passed through compressor 2 to compress it to about 6 atmospheres, and arrives by conduit 3 at regenerator 4, which is one of the series of transposable regenerators 4 to 7, through valve 411, which is one of the series of valves 4a to 7a that control communication between conduit 3 and the regenerators.
  • regenerator 4 which is one of the series of transposable regenerators 4 to 7, through valve 411, which is one of the series of valves 4a to 7a that control communication between conduit 3 and the regenerators.
  • the deeply cooled air passes through a transposable valve or part of double check valve 4a, which is one of the series of such valves 4d to 7d for delivery through conduit 8 to the lower part of pressure column 9 which, in conjunction with the low pressure column 10, forms a double rectifier tower arrangement.
  • the liquid in the sump of the pressure column which is under a pressure of about 5.6 atm., is delivered from the bottom of the column by conduit 11 to adsorber 12, thence to heat exchanger 13 from Where it passes through conduit 14 and expansion valve 15 to the middle portion of the low pressure column 10 in which the pressure is about 1.4 atm.
  • an impure nitrogen fraction is removed by conduit 16 and is passed through the transposable valve 72, which is one of the series of valves 4e to 7e, for delivery to regenerator 7 of the series 4 to 7.
  • the greater portion of this fraction passes through transposable valve 7c, which is one of the series of valves 40 to 7c, and then through conduit 17 to the compressor 18 for compression to about atm.
  • the compressed gas leaves the compressor via conduit 19, and preferably passes through an adsorber 20 having a bypass valve 21, to a group of heat exchangers 23, 24 and 25 and from there passes through the collecting conduit 26 to heat exchanger 27.
  • the circulating nitrogen passes on the one side through conduit 28 and through heat exchangers 29 and 30 and through conduit 31 to the collecting conduit 32, while on the other side it passes through conduit 33, heat exchanger 34 and conduit 35 to the same collecting conduit 32.
  • nitrogen is withdrawn through conduit 42 and through heat exchanger 39, conduit 43, heat exchanger 13 and conduit 44 3 and through the two valves 5d and 6d of the series M to 7d, and passes as scavenging gas through two transposable regenerators 5 and 6 of the series 4 to 7 in which it is warmed to the temperature of the surroundings.
  • the scavenging gas then passes through the two valves 51) and 6b of the series 4/) to 7b and makes its exit through conduit as impure nitrogen gas.
  • each regenerator in a first phase of operation is traversed in a downward direction by air to be cooled therein to a low temperature in preparation for its fractionation, in a second and third phase in an upward direction by scavenging gas which is to be warmed therein while effecting sublimation of the CO and of ice formations, and in a fourth phase in an upward direction by circulating nitrogen that is to be warmed.
  • a portion of the circulating nitrogen fraction is advantageously diverted from the lower half of the corresponding regenerators through valve 7 f of the series of valves 4] to 7f and is delivered through conduit 46 having valve 47 therein and through conduit 48 to the expansion turbine 49.
  • the expanded gas then passes through conduit 50 to the collection conduit 44 for scavenging gas.
  • a portion of the impure nitrogen can be diverted from the circulation conduit 16 by Way of conduit 51 for passage through heat exchanger 34 and conduit 52 having therein valve 53 and then through conduit 48 to the expansion turbine 49.
  • the regulation is determined by the temperature equilibrium which must be maintained during the process.
  • liquid oxygen is removed by conduit 54, is compressed to about 41 atm. by pump 55, and is delivered b conduit 56 to a series of heat exchangers 29, 27 and 23 in which the liquid oxygen is brought to about the temperature of the surroundings for delivery under about 40 atm. by conduit 57 having therein valve 58 to its destination.
  • a portion of the liquid nitrogen is diverted from conduit 66 by conduit 69 with valve 70 directly to conduit 71 which draws gas from the head of the washing column 68 to produce a stoichiometric mixture for ammonia synthesis.
  • the conduit 71 then delivers the hydrogen-nitrogen mixture through heat exchangers 61 and 72, conduits 73 and 74, heat exchangers 75 and 25, and then through conduits 76 and 77 to the collecting conduit 78 having therein valve 79 for delivery of the hydrogen-nitrogen mixture to an ammonia synthesis plant under a pressure of about 24 atm.
  • a hydrogen rich gas such as converter gas is delivered by conduit 80 to compressor 81, and thence by conduit 82 and heat exchanger 83, which can be water-cooled, and by conduit 84 to heat exchanger 75, then through conduit 85 to heat exchanger 72, and from there through conduit 86 to heat exchanger 87. From heat exchanger 87 the gas is delivered by conduit 88 to the cooling coil 89 in heat exchanger 63 and from there by conduit 90 to the lower portion of the washing column 68.
  • the liquid nitrogen with impurities consisting mainly of CO is taken from the sump of the washing column 68 by conduit 91 with expansion valve 92 therein for passage through heat exchangers 63 and 87, conduit 93, heat exchanger 30, conduit 94, heat exchanger 24, and then to conduit 95 for delivery to the Outside.
  • streams (1), (2), and (3) are heat exchanged with the pure nitrogen fluid.
  • streams (1), (2), and (3) are heat exchanged with the pure nitrogen fluid.
  • a method of fractionating air comprising: compressing air and passing the compressed air in one direction through a first regenerator means to the high pressure part of a double rectifying column near the bottom thereof, withdrawing liquid from the bottom of said high pressure column and delivering it to an intermediate point in the low pressure part of said double rectifying column, withdrawing nitrogen from the top of said low pressure column and passing said nitrogen through at least a second regenerator means to be scavenged in the direction opposite to said one direction, withdrawing impure nitrogen from a middle section of said high pressure column at a point wherein said impure nitrogen is not of sufficient purity for ammonia synthesis, and passing the impure nitrogen through a further regenerator means in the direction opposite to said one direction, compressing at least a part of the impure nitrogen after passing the same through said further regenerator means, drawing liquid oxygen from the bottom of said low pressure column compressing said liquid oxygen and exchanging heat between the evaporating compressed oxygen and the compressed impure nitrogen, the latter being thereby at least partly liquefied, and returning the at least partly liquefie
  • a method as defined by claim 10 further comprising the steps of withdrawing pure condensed liquid nitrogen from the top zone of the high pressure column, and combining said liquid with said pure gaseous nitrogen for flow to ammonia synthesis.
  • both said pure gaseous nitrogen and said pure condensed liquid are of suflicient purity for ammonia synthesis gas, the point of withdrawing said pure condensed liquid being above the point of withdrawing said impure nitrogen, said pure gaseous fraction and said pure liquid fraction being passed to the ammonia synthesis plant without any further rectification.
  • a method of fractionating air comprising: compressing air and passing the compressed air in one direction through a first regenerator means to the high pressure part of a double rectifying column near the bottom thereof, withdrawing liquid from the bottom of said high pressure column and delivering it to an intermediate point in the low pressure part of said double rectifying column, withdrawing nitrogen from the top of said low pressure column and passing said nitrogen through at least a second regenerator means to be scavenged in the direction opposite to said one direction, withdrawing impure nitrogen from a middle section of said high pressure column and passing the impure nitrogen through a further regenerator means in the direction opposite to said one direction, compressing at least a part of the impure nitrogen after passing the same through said further regenerator means, drawing liquid from the bottom of said low pressure column, compressing said liquid oxygen and exchanging heat between evaporating compressed oxygen and the compressed impure nitrogen thereby at least partly liquefied, and returning the impure nitrogen to said high pressure column near the point of withdrawal of the impure nitrogen from the column, withdrawing pure nitrogen from the head of said high pressure
  • streams (l), (2), and (3) are heat exchanged with pure nitrogen.
  • streams (1), (2), and (3) are heat exchanged with pure nitrogen.
  • a method of fractionating air comprising: compressing air and passing the compressed air in one direction through a first regenerator means to the high pressure part of a double rectifying column near the bottom thereof, withdrawing liquid from the bottom of said high pressure column and delivering it to an intermediate point in the low pressure part of said double rectifying column, withdrawing nitrogen from the top of said low pressure column and passing said nitrogen through at least a second regenerator means to be scavenged in the direction opposite to said one direction, withdrawing impure nitrogen from a middle section of said high pressure column and passing the impure nitrogen through a further regenerator means in the direction opposite to said one direction, compressing at least a part of the impure nitrogen after passing the same through said further regenerator means, exchanging heat between said compressed impure nitrogen and one or more streams from a plant for producing ammonia synthesis gas by scrubbing crude hydrogen with liquid nitrogen, said streams comprising (a) a mixture of nitrogen and carbon monoxide, and (b) pure ammonia synthesis gas, drawing liquid oxygen from the bottom of said low pressure column compress
  • first regenerator means means to compress air and pass it through said first regenerator means to chill the air, a double rectification column with a high pressure and a low pressure portion connected near the bottom of the high pressure portion to said first regenerator means to receive the chilled air therefrom, at least a second regenerator means, means for withdrawing nitrogen from the head of said low pressure column and for passing said nitrogen through said at least second regenerator means to scavenge said regenerator means, means for withdrawing impure nitrogen from a middle section of said high pressure rectifying column and for passing said impure nitrogen through a further regenerator means to be warmed, means for compressing the warmed impure nitrogen employed for cooling the further regenerator means, means for at least partly liquefying the compressed nitrogen, and means including a throttle valve for returning the at least partly liquefied nitrogen to said column near the point thereof from which it was withdrawn from the column, conduit means leading from the head of the high pressure portion of said column for drawing pure nitrogen therefrom, said conduit means comprising two

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US3596470A (en) * 1965-05-18 1971-08-03 Linde Ag Process and apparatus for the low-temperature separation of a hydrogen-rich gas mixture
US4372764A (en) * 1980-07-22 1983-02-08 Air Products And Chemicals, Inc. Method of producing gaseous oxygen and a cryogenic plant in which said method can be performed
US4957524A (en) * 1989-05-15 1990-09-18 Union Carbide Corporation Air separation process with improved reboiler liquid cleaning circuit
US5355681A (en) * 1993-09-23 1994-10-18 Air Products And Chemicals, Inc. Air separation schemes for oxygen and nitrogen coproduction as gas and/or liquid products
US5355682A (en) * 1993-09-15 1994-10-18 Air Products And Chemicals, Inc. Cryogenic air separation process producing elevated pressure nitrogen by pumped liquid nitrogen
US5505052A (en) * 1993-06-07 1996-04-09 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and unit for supplying a gas under pressure to an installation that consumes a constituent of air
EP0979983A1 (de) * 1998-08-13 2000-02-16 Air Products And Chemicals, Inc. Vorbehandlung des Rohgases bei der Synthesegasherstellung
DE102007031759A1 (de) 2007-07-07 2009-01-08 Linde Ag Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft
DE102007031765A1 (de) 2007-07-07 2009-01-08 Linde Ag Verfahren zur Tieftemperaturzerlegung von Luft
DE102009034979A1 (de) 2009-04-28 2010-11-04 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Erzeugung von gasförmigem Drucksauerstoff
EP2312248A1 (de) 2009-10-07 2011-04-20 Linde Aktiengesellschaft Verfahren und Vorrichtung Gewinnung von Drucksauerstoff und Krypton/Xenon
EP2458311A1 (de) 2010-11-25 2012-05-30 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102010052544A1 (de) 2010-11-25 2012-05-31 Linde Ag Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2520886A1 (de) 2011-05-05 2012-11-07 Linde AG Verfahren und Vorrichtung zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2568242A1 (de) 2011-09-08 2013-03-13 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Stahl
EP2600090A1 (de) 2011-12-01 2013-06-05 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Erzeugung von Drucksauerstoff durch Tieftemperaturzerlegung von Luft
DE102011121314A1 (de) 2011-12-16 2013-06-20 Linde Aktiengesellschaft Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102013017590A1 (de) 2013-10-22 2014-01-02 Linde Aktiengesellschaft Verfahren zur Gewinnung eines Krypton und Xenon enthaltenden Fluids und hierfür eingerichtete Luftzerlegungsanlage
DE102012017488A1 (de) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren
EP2784420A1 (de) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Verfahren zur Luftzerlegung und Luftzerlegungsanlage
WO2014154339A2 (de) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Verfahren zur luftzerlegung und luftzerlegungsanlage
EP2801777A1 (de) 2013-05-08 2014-11-12 Linde Aktiengesellschaft Luftzerlegungsanlage mit Hauptverdichterantrieb
EP2963369A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und vorrichtung zur tieftemperaturzerlegung von luft
EP2963371A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und vorrichtung zur gewinnung eines druckgasprodukts durch tieftemperaturzerlegung von luft
EP2963367A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch
EP2963370A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und vorrichtung zur tieftemperaturzerlegung von luft
WO2021102248A1 (en) * 2019-11-20 2021-05-27 Oakbio, Inc. Bioreactors with integrated catalytic nitrogen fixation
US12247194B2 (en) 2019-11-20 2025-03-11 Oakbio, Inc. Bioreactors with integrated catalytic nitrogen fixation

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* Cited by examiner, † Cited by third party
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DE102016107468B9 (de) * 2016-04-22 2017-12-21 Fritz Winter Eisengiesserei Gmbh & Co. Kg Verfahren und Anlage zur Nutzung eines von einer Gaszerlegeeinrichtung bereitgestellten Zielgases

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2526996A (en) * 1947-02-21 1950-10-24 Elliott Co Method and apparatus for separating mixed gases
US2895304A (en) * 1955-06-02 1959-07-21 Linde Eismasch Ag Process and apparatus for gas purification
US2936593A (en) * 1956-04-27 1960-05-17 Air Liquide Process for the production of ammonia synthesis gas
US2962867A (en) * 1956-09-20 1960-12-06 Linde Eismasch Ag Process for decomposing hydrogencontaining gas mixtures
US3216206A (en) * 1961-11-29 1965-11-09 Linde Eismasch Ag Low temperature distillation of normally gaseous substances

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE935195C (de) * 1954-05-26 1955-11-17 Linde Eismasch Ag Verfahren zur Herstellung von fluessigem Sauerstoff aus Luft und Vorrichtung zu seiner Durchfuehrung
DE955867C (de) * 1955-06-02 1957-01-10 Linde Eismasch Ag Verfahren zum Trennen eines verdichteten, wasserstofreichen Gasgemisches
DE1103363B (de) * 1958-09-24 1961-03-30 Linde Eismasch Ag Verfahren und Vorrichtung zur Erzeugung eines ausgeglichenen Kaeltehaushaltes bei der Gewinnung von unter hoeherem Druck stehenden Gasgemischen und/oder Gasgemisch-komponenten durch Rektifikation
DE1098970B (de) * 1959-07-20 1961-02-09 Linde S Eismaschinen Ag Zweign Verfahren und Einrichtung zur Kaelteerzeugung durch arbeitsleistende Entspannung
DE1092494B (de) * 1959-07-29 1960-11-10 Linde S Eismaschinen Ag Zweign Verfahren und Einrichtung zur Kaelteerzeugung durch arbeitsleistende Entspannung eines Hochdruckgases

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2526996A (en) * 1947-02-21 1950-10-24 Elliott Co Method and apparatus for separating mixed gases
US2895304A (en) * 1955-06-02 1959-07-21 Linde Eismasch Ag Process and apparatus for gas purification
US2936593A (en) * 1956-04-27 1960-05-17 Air Liquide Process for the production of ammonia synthesis gas
US2962867A (en) * 1956-09-20 1960-12-06 Linde Eismasch Ag Process for decomposing hydrogencontaining gas mixtures
US3216206A (en) * 1961-11-29 1965-11-09 Linde Eismasch Ag Low temperature distillation of normally gaseous substances

Cited By (34)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3596470A (en) * 1965-05-18 1971-08-03 Linde Ag Process and apparatus for the low-temperature separation of a hydrogen-rich gas mixture
US4372764A (en) * 1980-07-22 1983-02-08 Air Products And Chemicals, Inc. Method of producing gaseous oxygen and a cryogenic plant in which said method can be performed
US4957524A (en) * 1989-05-15 1990-09-18 Union Carbide Corporation Air separation process with improved reboiler liquid cleaning circuit
US5505052A (en) * 1993-06-07 1996-04-09 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and unit for supplying a gas under pressure to an installation that consumes a constituent of air
US5355682A (en) * 1993-09-15 1994-10-18 Air Products And Chemicals, Inc. Cryogenic air separation process producing elevated pressure nitrogen by pumped liquid nitrogen
US5355681A (en) * 1993-09-23 1994-10-18 Air Products And Chemicals, Inc. Air separation schemes for oxygen and nitrogen coproduction as gas and/or liquid products
EP0979983A1 (de) * 1998-08-13 2000-02-16 Air Products And Chemicals, Inc. Vorbehandlung des Rohgases bei der Synthesegasherstellung
DE102007031759A1 (de) 2007-07-07 2009-01-08 Linde Ag Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft
DE102007031765A1 (de) 2007-07-07 2009-01-08 Linde Ag Verfahren zur Tieftemperaturzerlegung von Luft
EP2015012A2 (de) 2007-07-07 2009-01-14 Linde Aktiengesellschaft Verfahren zur Tieftemperaturzerlegung von Luft
EP2015013A2 (de) 2007-07-07 2009-01-14 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft
DE102009034979A1 (de) 2009-04-28 2010-11-04 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Erzeugung von gasförmigem Drucksauerstoff
EP2312248A1 (de) 2009-10-07 2011-04-20 Linde Aktiengesellschaft Verfahren und Vorrichtung Gewinnung von Drucksauerstoff und Krypton/Xenon
EP2466236A1 (de) 2010-11-25 2012-06-20 Linde Aktiengesellschaft Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tiefemperaturzerlegung von Luft
DE102010052544A1 (de) 2010-11-25 2012-05-31 Linde Ag Verfahren zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2458311A1 (de) 2010-11-25 2012-05-30 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102010052545A1 (de) 2010-11-25 2012-05-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2520886A1 (de) 2011-05-05 2012-11-07 Linde AG Verfahren und Vorrichtung zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2568242A1 (de) 2011-09-08 2013-03-13 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Stahl
DE102011112909A1 (de) 2011-09-08 2013-03-14 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Stahl
EP2600090A1 (de) 2011-12-01 2013-06-05 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Erzeugung von Drucksauerstoff durch Tieftemperaturzerlegung von Luft
DE102011121314A1 (de) 2011-12-16 2013-06-20 Linde Aktiengesellschaft Verfahren zur Erzeugung eines gasförmigen Sauerstoff-Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102012017488A1 (de) 2012-09-04 2014-03-06 Linde Aktiengesellschaft Verfahren zur Erstellung einer Luftzerlegungsanlage, Luftzerlegungsanlage und zugehöriges Betriebsverfahren
EP2784420A1 (de) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Verfahren zur Luftzerlegung und Luftzerlegungsanlage
WO2014154339A2 (de) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Verfahren zur luftzerlegung und luftzerlegungsanlage
EP2801777A1 (de) 2013-05-08 2014-11-12 Linde Aktiengesellschaft Luftzerlegungsanlage mit Hauptverdichterantrieb
DE102013017590A1 (de) 2013-10-22 2014-01-02 Linde Aktiengesellschaft Verfahren zur Gewinnung eines Krypton und Xenon enthaltenden Fluids und hierfür eingerichtete Luftzerlegungsanlage
EP2963369A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und vorrichtung zur tieftemperaturzerlegung von luft
EP2963371A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und vorrichtung zur gewinnung eines druckgasprodukts durch tieftemperaturzerlegung von luft
EP2963367A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch
EP2963370A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und vorrichtung zur tieftemperaturzerlegung von luft
WO2016005031A1 (de) 2014-07-05 2016-01-14 Linde Aktiengesellschaft Verfahren und vorrichtung zur tieftemperaturzerlegung von luft mit variablem energieverbrauch
WO2021102248A1 (en) * 2019-11-20 2021-05-27 Oakbio, Inc. Bioreactors with integrated catalytic nitrogen fixation
US12247194B2 (en) 2019-11-20 2025-03-11 Oakbio, Inc. Bioreactors with integrated catalytic nitrogen fixation

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