US3083544A - Rectification of gases - Google Patents

Rectification of gases Download PDF

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US3083544A
US3083544A US841749A US84174959A US3083544A US 3083544 A US3083544 A US 3083544A US 841749 A US841749 A US 841749A US 84174959 A US84174959 A US 84174959A US 3083544 A US3083544 A US 3083544A
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gas
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pressure
exchanger
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Jakob Fritz
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Linde GmbH
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Gesellschaft fuer Lindes Eismaschinen AG
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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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • 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
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—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
    • F25J3/04339—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 air
    • 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
    • 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
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • 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
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air

Definitions

  • This invention relates to the art of rectifying gaseous mixtures, and is concerned with the provision of a process and apparatus for obtaining a balanced cold economy in the production of gas mixtures and/ or gas mixture components, which are under a higher pressure, through rectification.
  • the known methods for obtaining a balanced cold economy in the production of oxygen, which is under an elevated pressure involve the rectification of air by extraction in the liquid state and bringing it to the desired gaseous pressure state, for example, tempered to ambient air; compressing an amount of gastal en from the preliminary rectification and heated again in counterfiow in the heat exchangers for the incoming air-to a high pressure, before it is fed to the liquid oxygen, compressed to a higher pressure, for its evaporation and heating; and transforming it subsequently (if necessary, after additional heat exchange and expansion) into the preliminary or lowpressure rectification.
  • This method requires the arrangement of high-pressure compressors whose particular disadvantage is the contamination of the gases by oil and moisture. Besides, the high-pressure compressors are very expensive, and are uneconomical in operation.
  • the method for obtaining a balanced cold economy in the production of compressed gaseous mixtures and/ or gas mixture compon cuts from the rectification of one or several gas mixtures by extraction in the liquid low-pressure stage and by bringing them to the desired gaseous, mediumor high-pressure state, for example, tempered to ambient air is characterized in that an amount of gas is taken from the preliminary rectification, heated in counterfiow to the incoming gas mixture, cooled by heat exchange for evaporation and heating of the liquid component, compressed to a higher pressure, and subjected to partial heating and subsequent work-producing expansion, after the liquefied components have been separated and returned.
  • this new method has the advantage that the gas taken from the preliminary rectification is brought, without pressure increase, by heat exchange to the component compressed to a higher pressure, and expanded work-producingly after partial heating.
  • This gas is thus maintained in its pure state and requires no further treatment. It is not particularly characteristic of the process according to the invention where the expanded gas is conducted, but preferably it can be conducted to the lowpressure rectification or at least partly exhausted, if nec essary after further heat exchange in counterfiow with production gases, and after heating in the regenerators, etc.
  • the partial heating of the gas before the workproducing expansion is effected preferably by heat exchange with a compressed gas of a so-called closed or open medium-pressure circuit.
  • the quantity of gas effecting the partial heating for the work-producing expansion has its pressure reduced and is subjected to rectification, for example, in the preliminary or in the low-pressure stage. Compression under medium pressure preceded by heating and followed by cooling of the gas in counter-flow to itself conveniently forms a closed medium-pressure circuit. But if the gas which efiects the partial heating of the gas destined for work-producing expansion is compressed to a pressure suitable for obtaining the desired compressed gas mixture under higher pressure, liquefied, supercooled, fed to the rectifying and washing device for said gas mixture and then mixed with the resulting gas mixture, one has an example of an open medium-pressure circuit.
  • These medium-pressure circuits in which the pressure rarely attains or exceeds 30 atmospheres absolute, are of particular advantage because of the possibility of using dry-running compressors, since the gas to be compressed is not contaminated and, therefore, needs no after-treatment or complicated purification.
  • An open medium-pressure circuit may, however, be accompanied by a displacement of cold, so that in order to return it from the rectification of one gas mixture to that of the other, an amount of gas must be extracted from the preliminary rectification, liquefied in indirect heat-exchange against the gas mixture formed by the supply of a part of the liquefield gas effecting the partial heating, and subjected again to a preliminary rectification.
  • Another possibility of exchanging cold between the two gas mixtures taken from a rectification of each consists in that the complete heating of the component brought to a higher pressure and the preliminary cooling of the compressed gas mixture which is to be separated is eifected in mutual heat exchange, preferably by the interposition of a so-called brine circuit, because of the fire and explosion hazard.
  • FIG. 1 is a diagrammatic representation of an apparatus organization for carrying out the above-described process, with particular applicability to the separation of the components of air;
  • PEG. 2 is a diagrammatic representation of a modified form of the apparatus organization shown in FIG. 1;
  • FIG. 3 is a diagrammatic representation of a further modification of the apparatus organization shown in FIG. 1, with particular applicability to the provision of compressed nitrogen for production of synthetic ammonia gas.
  • FIGURE 1 shows the most important parts of an apparatus for the decomposition of gas mixtures, air being used as the example.
  • the apparatus consists essentially of an intake pipe 1 for air compressed to about 5.3 to 6.5 atmospheres absolute; a pair or" periodicallly reversible regenerators 2 for cooling the incoming air; a connecting pipe 3 to the sump of a rectifying column 4, with a pressure column 5; a lowpressure column 6 and a condenser 7; a line 8, with an expansion valve 9, from the sump of the pressure column 5, to the low-pressure column 6 for the liquefied gas mixture; a pipe ill, with an expansion valve 11, from the pressure side of the condenser '7 to the head of the lowpressure column 6, for liquefied nitrogen with connected counter-flow heat exchanger 12, an extraction pipe extending through this to the regenerators 2; a second interposed counterfiow heat exchanger 14; a discharge pipe 15 for the nitrogen produced; an extraction pipe 16, from the low-pressure part of the condenser 7, for liquid oxygen; a liquid gas pump 17 for compressing oxygen to the desired higher pressure; a pressure pipe 18 to a counterfiow heat
  • the medium-pressure circuit represented by the parts .32, 33, 34, 35, 3'6, 37, 38 and 39, which is self-contained by the extension into the parts 3, 5 and 21, is arranged because the regenerators 2 work with excess discharge .so that there is no excess heat available that can be used for heating the air to be expanded in the turbine 29.
  • the partial heating of the air to be expanded in the turbine 29 is therefore effected in the counter-flow heat exchanger 27, which is interposed in the medium pressure circuit, by taking over the heat of liquefaction from the air conducted in the medium-pressure circuit.
  • the amount of air issuing from the separator 24 is not sufli c-ient to produce the necessary cold in the work-producing expansion taking place after the partial heating, the amount is increased by adding pressure-column air by way of the pipe and the valve 41.
  • a portion (usually a small portion) of the expanding air is injected into the low-pressure column, another (usually larger) portion is added to the nitrogen issuing through the pipe 13 by Way of the branch line 31.
  • FIGURE 2 shows, in a practically identical device for carrying out the same process, a'variation in the arrangement of the medium-pressure circuit, according'to which variation instead of a medium-pressure circuit for air from the pressure column, a closed medium-pressure circuit for nitrogen from the pressure column-is provided.
  • .Nitrogen is extracted from the condenser 7, through the pipe 51, of the pressure column 5: it is heated in the heatexchangerSZ and conducted through the line 53 to 'the medium-pressure, dry-running compressor 54, aftercooled and cooled by the line 55 in the heat exchanger 52 in counterflow to itself, conducted through the line 56 to the counterflow heat exchanger 27 for liquefaction, where the partial heating of the air to be expanded is eflected, and returned to the pressure column 5 through the line 57 and the expansion valve 58.
  • FIGURE 3 shows the connection of an air separation plant 61 for the production of compressed oxygen and compressed nitrogen with a gas separation plant 62, for the production of synthetic ammonia gas from converter gas which consists of hydrogen, nitrogen, carbon monoxide and methane.
  • the oxygen is to be supplied with a pressure of about 40 atmospheres, and the nitrogen is to be brought to the pressure of the crude gas, that is, about 25 atmospheres.
  • the nitrogen which must, in any event, be transferred to the gas plant, that is, the production nitrogen.
  • the production nitrogen is extracted in the line 63 from the pressure column 5, under its pressure, conducted in counterfiow to the incoming air in spirals 64 and heated, brought outside the separation apparatus, for example, by means of the dry-running compressor 65 to about 25 atmospheres absolute, andis subjected to a heat exchange, after recooling in an after-cooler (not shown) in counterflow with the residual gas arriving from the gas plant and with the hydrogen-nitrogen mixture. It is cooled, in the counterflow heat exchangers: and 67, approximately to the start of its liquefaction, and then liquefied in the counterflow heat exchanger 68, thereby giving ofi" again (as in the preceding example) its heat of liquefaction to the air to be expanded in the turbine 29.
  • This nitrogen which is liquefied in the counterfiow heat exchanger 68, is slightly supercooled in the counterflow heat exchanger 69 against residual gas, and then arrives through the line 70 in the liquid state in the gas plant 62, where one part of is used for washing in the wash column 71 while the other part is fed directly to the hydrogen-nitrogen mixture in 72.
  • the crude gas is cooled in the counterflow heat exchangers 73 and 74, in counterflow with the hydrogennitrogen mixture issuing through the line 75.
  • a The crude gas arrives in line 76, and is cooled in a counterflowprecooler 73 to about '5? C. and the condensed water is stripped off in the separator 77.
  • the gas is cooled to about 5 0 C. It then enters a gel drier and from there-in the counterflow heat exchangers proper 79 and 8.0, namely the hot leg (79) and the cold leg (80). From the cold leg 80 it is V transferred to the evaporating vessel 81, where it is cooled to a constant temperature of about K.
  • a brine circuit is interposed between the oxygen line 29 and the counterflow heat exchanger 73 and 74 of the gas separation part.
  • This brine circuit 86 transfers the cold-still contained in the oxygenover the heat exchanger 37 to the crude gas and serves to precool the crude gas. Because the compressed oxygen leaves the counterfiow heat-exchanger "19 relatively cold in this method of low-pressure heat e x- 'change, the great cold supply can be utilized with advantage and the otherwise necessary cooling by ammonia, which requires energy, can be avoided.
  • the method of producing cold which comprises withdrawing a component of a gas mixture to ,be separated from a rectifying column at low' pressure in the .liquid's'tate,
  • the method of producing cold which comprises withdrawing oxygen from a rectifying column at low pressure in the liquid state, pumping said liquid to said high pressure; withdrawing a gas from the preliminary rectification column and heating it in counter-flow to the incoming gas mixture, vaporizing said high pressure liquid by heatexchange with said gas, thereby condensing said gas at least partially to form a liquid part and a gaseous part thereof, separating the gaseous part from the condensed and liquefied part of said gas, leading the liquefied part of said gas into said preliminary rectification column, warming the gaseous part of said gas and expanding it by the production of external work.
  • Apparatus for the separation of gas mixtures comprising a conventional gas separation device with a twocolumn rectifying device and a regenerator arrangement for heat-exchange and cooling of the gas mixture, at gas conduit connecting the lower part of the high pressure column of said rectifying device with the cold ends of heating coils inside the regenerators, a pump connected to the sump of the low pressure column, a heat-exchanger for evaporating the high pressure liquid, means connecting the high pressure side of said pump to said heat-exchanger, means connecting the warm ends of said heating coils to the second channel of said heat-exchanger, means connecting the cold end of said second channel to a liquid separator, conduit means for returning the condensate from said separator to the pressure column, gas lines from the upper end of said separator to the cold end of a second heat-exchanger, means for passing compressed gas through the second channel of said second heat-exchanger, means connecting the warm end of said second heat-exchanger with the inlet of an expansion turnine and means connecting the outlet of said turbine with
  • Apparatus according to claim 3 in connection with another gas separation unit consisting of heatexchangers for cooling a gas to be washed and a washing device, the connection consisting of means connecting the head of the high pressure column of the conventional gas separation device with heating coils contained in the regenerators, means connecting the warm ends of said coils with a compressor and an aftercooler, means connecting the aftercooler with a heat-exchanging line conducting through one first heat-exchanger as well as another first heat-exchanger connected to the one heat-exchanger in parallel and from there through said second heat-exchanger and from there through a third heat-exchanger, means connecting said heat-exchanging line with an expansion device and with a condenser of said washing device, means connecting said expansion device with said high pressure column, means connecting the foot of the washing tower of said other separation unit with said third heat-exchanger, means connecting said third heatexchanger with the one of said two first-exchangers, means connecting said washing device with the other of said two first heat-exchangers.
  • Apparatus for the separation of gas mixtures comprising a conventional gas sepanation device with a twocolumn rectifying device and a regenerator arrangement for heatexchange and cooling of the gas mixture in connection with another gas separation unit consisting of heat exchangers for cooling a gas to be washed and a washing device, a gas conduit connecting the lower part of the high-pressure column of said rectifying device with the cold ends of heating coils inside the regenerators, a pump connected to the sump of the low-pressure column of said rectifying device, a heat-exchanger for evaporating high-pressure liquid, means connecting the highpressure side of said pump to said heat-exchanger, means connecting the warm ends of said heating coils to a second channel of said heat-exchangers, means connecting the cold end of said second channel to a liquid separator, conduit means for returning condensate from said separator to the pressure column, gas lines from the upper end of said separator to the cold end of a second heatexchanger, means for passing compressed gas through a second channel of
  • Apparatus for the separation of gas mixtures comprising .a conventional gas separation device with a twocolumn rectifying device and a regenerator arrangement for heat-exchange and cooling of the gas mixture in connection with another gas separation unit consisting of heat exchangers for cooling a gas to be 'washed and a washing device, a gas conduit connecting the lower part of the high-pressure column of said rectifying device with'the cold ends of heating coils inside the regenenators, a pump connected to the sump of the low-pressure column of said rectifying device, a heat-exchanger for evaporating high-pressure liquid, meansconnecting the high-pressure side of said pump to said heat-exchanger, means connecting the warm ends of said heating coils to a second channel of said heat-exchangers, means connecting the cold end of said second channel 'to a liquid separator, conduit means for returning condensate from said separator'to the pressure column, gas lines from the upper end of said separator to the cold end of a second heat-exchanger,

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  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
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Cited By (29)

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US3214925A (en) * 1960-08-13 1965-11-02 Linde Eismasch Ag System for gas separation by rectification at low temperatures
US3216206A (en) * 1961-11-29 1965-11-09 Linde Eismasch Ag Low temperature distillation of normally gaseous substances
US3261168A (en) * 1961-11-03 1966-07-19 Petrocarbon Dev Ltd Separation of oxygen from air
US3327487A (en) * 1963-03-21 1967-06-27 Ernst karwat
US4099945A (en) * 1975-10-28 1978-07-11 Linde Aktiengesellschaft Efficient air fractionation
JPS55152374A (en) * 1979-05-18 1980-11-27 Hitachi Ltd Air separation
EP0029656A1 (de) * 1979-10-23 1981-06-03 Air Products And Chemicals, Inc. Verfahren und kryogenische Anlage für die Herstellung gasförmigen Sauerstoffs
US4279631A (en) * 1975-08-06 1981-07-21 Linde Aktiengesellschaft Process and apparatus for the production of oxygen by two-stage low-temperature rectification of air
US4303428A (en) * 1979-07-20 1981-12-01 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic processes for separating air
EP0042676A1 (de) * 1980-06-17 1981-12-30 Air Products And Chemicals, Inc. Verfahren zur Herstellung gasförmigen Sauerstoffs und kryogenische Anlage zur Durchführung dieses Verfahrens
DE102007031765A1 (de) 2007-07-07 2009-01-08 Linde Ag Verfahren zur Tieftemperaturzerlegung von Luft
DE102007031759A1 (de) 2007-07-07 2009-01-08 Linde Ag 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
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
EP2963371A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und vorrichtung zur gewinnung eines druckgasprodukts durch tieftemperaturzerlegung von luft
EP2963370A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und vorrichtung zur tieftemperaturzerlegung von luft
EP2963369A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und vorrichtung zur tieftemperaturzerlegung von luft
EP2963367A1 (de) 2014-07-05 2016-01-06 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft mit variablem Energieverbrauch

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DE1263037B (de) * 1965-05-19 1968-03-14 Linde Ag Verfahren zur Zerlegung von Luft in einer Rektifikationssaeule und damit gekoppelterZerlegung eines Wasserstoff enthaltenden Gasgemisches
JPS5545825B2 (de) * 1973-02-22 1980-11-19

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US2827775A (en) * 1949-11-11 1958-03-25 Linde Eismasch Ag Process for separating a compressed gas mixture
US2708831A (en) * 1953-04-09 1955-05-24 Air Reduction Separation of air
US2822675A (en) * 1954-04-23 1958-02-11 Air Liquide Production of gaseous oxygen under pressure
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Cited By (35)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3214925A (en) * 1960-08-13 1965-11-02 Linde Eismasch Ag System for gas separation by rectification at low temperatures
US3261168A (en) * 1961-11-03 1966-07-19 Petrocarbon Dev Ltd Separation of oxygen from air
US3216206A (en) * 1961-11-29 1965-11-09 Linde Eismasch Ag Low temperature distillation of normally gaseous substances
US3327487A (en) * 1963-03-21 1967-06-27 Ernst karwat
US4279631A (en) * 1975-08-06 1981-07-21 Linde Aktiengesellschaft Process and apparatus for the production of oxygen by two-stage low-temperature rectification of air
US4099945A (en) * 1975-10-28 1978-07-11 Linde Aktiengesellschaft Efficient air fractionation
JPS55152374A (en) * 1979-05-18 1980-11-27 Hitachi Ltd Air separation
US4303428A (en) * 1979-07-20 1981-12-01 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic processes for separating air
EP0029656A1 (de) * 1979-10-23 1981-06-03 Air Products And Chemicals, Inc. Verfahren und kryogenische Anlage für die Herstellung gasförmigen Sauerstoffs
EP0042676A1 (de) * 1980-06-17 1981-12-30 Air Products And Chemicals, Inc. Verfahren zur Herstellung gasförmigen Sauerstoffs und kryogenische Anlage zur Durchführung dieses Verfahrens
DE102007031765A1 (de) 2007-07-07 2009-01-08 Linde Ag Verfahren zur Tieftemperaturzerlegung von Luft
DE102007031759A1 (de) 2007-07-07 2009-01-08 Linde Ag Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch 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
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
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
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
WO2014154339A2 (de) 2013-03-26 2014-10-02 Linde Aktiengesellschaft Verfahren zur luftzerlegung und luftzerlegungsanlage
EP2784420A1 (de) 2013-03-26 2014-10-01 Linde Aktiengesellschaft Verfahren zur Luftzerlegung und Luftzerlegungsanlage
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DE102013017590A1 (de) 2013-10-22 2014-01-02 Linde Aktiengesellschaft Verfahren zur Gewinnung eines Krypton und Xenon enthaltenden Fluids und hierfür eingerichtete Luftzerlegungsanlage
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