US20150316317A1 - Method and device for low-temperature air separation - Google Patents
Method and device for low-temperature air separation Download PDFInfo
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- US20150316317A1 US20150316317A1 US14/651,320 US201314651320A US2015316317A1 US 20150316317 A1 US20150316317 A1 US 20150316317A1 US 201314651320 A US201314651320 A US 201314651320A US 2015316317 A1 US2015316317 A1 US 2015316317A1
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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
- F25J3/04—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
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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
- 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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04854—Safety aspects of operation
- F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
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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
- 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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- 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
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- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
- F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
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- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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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
- F25J3/04436—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 at least a triple pressure main column system
- F25J3/04442—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 at least a triple pressure main column system in a double column flowsheet with a high pressure pre-rectifier
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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
- 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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
- F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
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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
- 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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
- F25J3/04884—Arrangement of reboiler-condensers
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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
- 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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/0489—Modularity and arrangement of parts of the air fractionation unit, in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
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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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/10—Boiler-condenser with superposed stages
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/40—One fluid being air
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/50—One fluid being oxygen
Definitions
- the invention relates to a method according to the preamble of Claim 1 .
- the distillation column system of the invention includes a two-column system (for example a classic Linde double column system) for nitrogen-oxygen separation having a high-pressure column and a low-pressure column, which are operatively interconnected for heat exchange.
- the operative interconnection for heat exchange between the high-pressure column and the low-pressure column, as a rule, is realized by a main condenser in which head gas of the high-pressure column is liquefied against evaporating sump liquid of the low-pressure column.
- the distillation column system can comprise further devices, for example for producing other air components, in particular inert gases, for example producing argon which includes at least one raw argon column, or producing krypton-xenon.
- the distillation column system also includes the heat exchangers which are assigned directly to them and, as a rule, are realized as condenser-evaporators.
- a “main heat exchanger”, in this case, serves for cooling the feed air in indirect heat exchange with return streams from the distillation column system. It can be formed by one single or several heat exchanger portions which are connected in parallel and/or in series, for example by one or several plate heat exchanger blocks.
- a secondary condenser which is also realized as a condenser-evaporator
- oxygen removed in the liquid state from the low-pressure column is evaporated at an only slightly increased oxygen pressure of between 1.5 and 6 bar, preferably between 2.7 and 4 bar.
- Part of the cooled feed air is liquefied against the evaporating oxygen.
- a heat exchanger in which a first condensing liquid stream enters into indirect heat exchange with a second evaporating liquid stream, is designated as a “condenses evaporator”.
- Each condenser-evaporator comprises a liquefaction chamber and an evaporation chamber which consist of liquefaction passages or evaporation passages.
- the condensing (liquefying) of a first liquid stream is carried out in the liquefaction chamber and the evaporation of a second liquid stream is carried out in the evaporation chamber.
- the evaporation chamber and the liquefaction chamber are formed by groups of passages which are operatively interconnected for heat exchange.
- a method is sought that is capable of generating large volumes of nitrogen along with the oxygen at the slightly increased oxygen pressure and at the same time of keeping the number of externally driven machines, in particular of the compressors, which are not driven by a turbine of the method as small as possible.
- the oxygen in this case, is to be generated either as pure oxygen with a purity of in excess of 99.5 mol-% or as non-pure oxygen with less purity, in particular with a purity of less than 98 mol-%.
- an arrangement that is as compact as possible is also to be obtained.
- the method according to the invention in contrast to the process of WO 2009 095188 A2, is preferably operated with a comparatively small amount of pre-liquefaction of the air; the liquid part of the feed air which is to be introduced into the distillation column system includes a maximum of 29 mol-% and is in particular between 23 and 29 mol-%.
- the secondary condenser, the head condenser and the precolumn are arranged one above the other.
- An arrangement of two elements “one above another” is to be understood here as the upper end of the lower of the two elements being situated at a lower geodetic height than the lower end of the upper of the two elements and the projections of the two elements into a horizontal plane intersecting.
- the two elements can be arranged precisely one above another, this means the axes of the two elements extend along the same vertical straight line.
- the operating pressure of the precolumn is preferably chosen such that it corresponds to the pressure of the second part stream of the air which is required for the oxygen evaporation in the secondary condenser.
- the operating pressure of the precolumn in the sump is preferably between 7.5 bar and 10.5 bar.
- the first gaseous nitrogen product can be removed under precolumn pressure (at the head of said column).
- Said pressure in this case, is approximately 9 bar.
- up to 30 mol-%, preferably between 5 and 25 mol-% of the feed air volume can be removed from the precolumn as a first gaseous nitrogen product.
- the invention relates above all (but not only) to the area of relatively small units with extensive packaged units where dispensing with additional compressors plays a key role both in the time and money spent on equipment and maintenance and on energy consumption.
- the main heat exchanger Because in the case of the invention only a relatively small portion of nitrogen is removed as a low-pressure nitrogen stream, the main heat exchanger has a correspondingly small volume and consequently there is a further reduction in the time and money spent on equipment.
- the secondary condenser is arranged above the precolumn and in a second variant it is arranged below the precolumn.
- the secondary condenser and the head condenser can be arranged in a common container.
- the container is realized as a vertical cylinder and comprises a tight horizontal intermediate floor between the two apparatuses.
- a second gaseous nitrogen product can be produced directly from the high-pressure column under, for example, between 5 and 6.5 bar, also without the use of a product compressor (and without low-pressure stages). This is particularly favorable when the customer requires nitrogen under different pressures which correspond approximately to the operating pressures of the precolumn and high-pressure column.
- both nitrogen products can be produced with different purities.
- In total (first and second gaseous nitrogen product) up to 50 mol-%, preferably between 25 and 50 mol-% of the feed air volume can be produced as a pressurized nitrogen product.
- a Claude turbine which is operated with a third part stream of feed air and expands into the high-pressure column.
- Said third part stream is not fully cooled in the main heat exchanger (that is not guided up to the cold end), but only up to an intermediate temperature.
- the corresponding expansion machine is preferably formed by an expansion turbine.
- Said expansion turbine can be coupled to a booster in which, in particular, the turbine stream (third part stream) is boosted upstream of the expansion for carrying out work.
- a smaller oxygen concentration in the raw oxygen fraction is preferably produced in the sump of the precolumn than in the sump of the high-pressure column.
- the two raw oxygen fractions are consequently not mixed with one another, but, according to claim 4 , are fed separately into the low-pressure column at different intermediate points. Between the two feed points there are, for example, between 5 and 20, preferably between 7 and 15 theoretical floors.
- the invention also relates to a device for the low-temperature separation of air according to claims 8 to 13 .
- FIG. 1 shows a first exemplary embodiment with a secondary condenser above the head condenser
- FIG. 2 shows a second exemplary embodiment with a secondary condenser below the precolumn
- FIG. 3 shows a third exemplary embodiment with the arrangement of a secondary condenser and head condenser in a common container.
- atmospheric air AIR
- main air compressor 202 via line 201 and compressed to a pressure of approximately 10 bar.
- the compressed feed air 203 is cooled in a precooling device 204 and then purified in a purification device 205 which includes molecular sieve absorbers, that means water and carbon dioxide in particular are removed.
- the compressed and purified feed air 206 is cooled to a first part 210 in a main heat exchanger 260 up to the cold end thereof.
- the “first part stream” 1 and the “second part stream” 2 a are formed from this.
- a “third part stream” 230 is recompressed in a booster compressor 466 with an aftercooler 467 , guided via line 231 also to the hot end of the main heat exchanger 260 , only cooled there however to an intermediate temperature and removed again.
- the cooled third part flow 232 is expanded in an expansion turbine 465 so as to carry out work and forwarded via line 233 .
- the expansion turbine 465 and the booster compressor 466 are coupled in a mechanical manner.
- the distillation column system includes a precolumn 10 , a pressure column 11 and a low-pressure column 12 as well as the condenser-evaporator linked thereto, the main condenser 13 and the head condenser 14 of the precolumn.
- the secondary condenser 46 is not part of the distillation column system.
- the distillation column system can also comprise an argon part which includes, in particular, at least one raw argon column and its head condenser; in addition, the argon part can comprise a pure argon column for separating argon and nitrogen.
- the separating columns for the separation of nitrogen and oxygen comprise the following operating pressures (in each case at the head):
- the cooled gaseous (or somewhat pre-liquefied) first part stream 1 of the feed air from the cold end of the main heat exchanger 260 is under a pressure which is just above the operating pressure of the precolumn 10 and is introduced directly into the precolumn above the sump.
- the precolumn 10 comprises a head condenser 14 , into the liquefaction chamber of which a nitrogen stream 31 is introduced.
- a liquid second part stream 2 b of the feed air (see below) is introduced into the evaporation chamber of the head condenser 14 of the precolumn 10 .
- the rest of the feed air is introduced into the distillation column system, in particular into the high-pressure column, via the line 233 in the gaseous state or substantially gaseous state.
- a gaseous stream 16 which is enriched in oxygen is removed from the evaporation chamber of the head condenser 14 and mixed with the gaseous air 233 .
- the streams 233 and 16 can be introduced separately (where applicable at different points) into the high-pressure column 11 .
- an additional liquid stream 4 is also directed into the evaporation chamber of the head condenser 14 . This is formed by part of the sump liquid of the precolumn 10 .
- the remainder 5 a, 5 b of the sump liquid of the precolumn is undercooled here in an undercooling heat exchanger 37 and introduced into the low-pressure column 12 , at an intermediate point above the feeding-in of the high-pressure column sump liquid 38 .
- the liquid 6 which is generated from part 31 of the head nitrogen 30 of the precolumn 10 in the condensation chamber of the head condenser 14 , is fed as head reflux into the precolumn 10 .
- Part 8 of the reflux liquid can be removed a little further down (as shown) and guided to the head of the high-pressure column 11 .
- the evaporated fraction 16 formed in the evaporation chamber of the head condenser 14 is guided via line 17 to the sump of the high-pressure column 11 , together with the third part stream 233 of the feed air which originates from the outlet of the Claude turbine 465 .
- the flushing liquid 32 a, 32 b from the head condenser 14 of the precolumn 10 is supplied to the high-pressure column 11 at an intermediate point in the lower region.
- the double column 11 / 12 / 13 functions in the generally known manner.
- liquid raw oxygen 33 at the sump and liquid non-pure nitrogen 35 from an intermediate point relatively high up are cooled in an undercooling heat exchanger 37 in indirect heat exchange with return streams and are introduced into the low-pressure column 12 via the lines 38 or 40 at the suitable points.
- the gaseous product streams are healed with feed air in the main heat exchange 260 indirect heat exchange.
- the main heat exchanger can consist of one block or of two or several blocks which are connected in parallel and/or in series.
- the oxygen 50 a removed in liquid form from the low-pressure column is pressurized in liquid form in a pump 55 to a pressure of, for example, between 2 and 5 bar, preferably between 2.7 and 4.0 bar, and is then directed via line 50 b into the evaporation chamber of the secondary condenser 46 .
- the evaporated oxygen 50 c is heated in the main heat exchanger to approximately ambient temperature and is finally ( 50 d ) produced as a gaseous oxygen product under medium pressure (MP GOX).
- the second part stream 2 a of the feed air is substantially fully liquefied in the liquefaction chamber of the secondary condenser.
- the liquefied second part stream 2 b is introduced into the evaporation chamber of the head condenser 14 of the precolumn 10 .
- Both condensers 14 and 46 of the exemplary embodiments are realized as bath evaporators, at least one plate heat exchanger block being arranged in a liquid bath.
- FIG. 2 differs from FIG. 1 in that the secondary condenser 46 is arranged below the precolumn 10 and the head condenser 14 .
- FIG. 3 differs from FIG. 1 in that the secondary condenser 46 and the head condenser 14 are arranged in a common container 301 .
- the container 301 is realized in a cylindrical manner and comprises a tight intermediate floor 302 . Said variant is slightly more compact than that of FIG. 1 and consequently needs less space. It also allows for even more cost-efficient production, more extensive prefabrication and easier transport of the components.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Power Engineering (AREA)
- Separation By Low-Temperature Treatments (AREA)
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP12008635.0 | 2012-12-27 | ||
EP12008635 | 2012-12-27 | ||
PCT/EP2013/003929 WO2014102014A2 (de) | 2012-12-27 | 2013-12-20 | Verfahren und vorrichtung zur tieftemperatur-luftzerlegung |
Publications (1)
Publication Number | Publication Date |
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US20150316317A1 true US20150316317A1 (en) | 2015-11-05 |
Family
ID=47562945
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US14/651,320 Abandoned US20150316317A1 (en) | 2012-12-27 | 2013-12-20 | Method and device for low-temperature air separation |
Country Status (6)
Country | Link |
---|---|
US (1) | US20150316317A1 (de) |
EP (1) | EP2938952A2 (de) |
AU (1) | AU2013369596A1 (de) |
MX (1) | MX2015008172A (de) |
RU (1) | RU2015130628A (de) |
WO (1) | WO2014102014A2 (de) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20170234614A1 (en) * | 2014-07-31 | 2017-08-17 | Linde Aktiengesellschaft | Method for the cryogenic separation of air and air separation plant |
WO2020083528A1 (de) * | 2018-10-23 | 2020-04-30 | Linde Aktiengesellschaft | Verfahren und anlage zur tieftemperaturzerlegung von luft |
US20220074656A1 (en) * | 2018-12-21 | 2022-03-10 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Apparatus and method for separating air by cryogenic distillation |
US20220252344A1 (en) * | 2019-07-10 | 2022-08-11 | Taiyo Nippon Sanso Corporation | Air separation device and air separation method |
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FR2831250A1 (fr) * | 2002-02-25 | 2003-04-25 | Air Liquide | Procede et appareil de separation d'air par distillation cryogenique |
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2013
- 2013-12-20 EP EP13826561.6A patent/EP2938952A2/de not_active Withdrawn
- 2013-12-20 AU AU2013369596A patent/AU2013369596A1/en not_active Abandoned
- 2013-12-20 WO PCT/EP2013/003929 patent/WO2014102014A2/de active Application Filing
- 2013-12-20 RU RU2015130628A patent/RU2015130628A/ru not_active Application Discontinuation
- 2013-12-20 MX MX2015008172A patent/MX2015008172A/es unknown
- 2013-12-20 US US14/651,320 patent/US20150316317A1/en not_active Abandoned
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WO2010142894A2 (fr) * | 2009-06-12 | 2010-12-16 | L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Appareil et procédé de séparation d'air par distillation cryogénique |
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US10480853B2 (en) * | 2014-07-31 | 2019-11-19 | Linde Aktiengesellschaft | Method for the cryogenic separation of air and air separation plant |
WO2020083528A1 (de) * | 2018-10-23 | 2020-04-30 | Linde Aktiengesellschaft | Verfahren und anlage zur tieftemperaturzerlegung von luft |
US11846468B2 (en) | 2018-10-23 | 2023-12-19 | Linde Gmbh | Method and unit for low-temperature air separation |
US20220074656A1 (en) * | 2018-12-21 | 2022-03-10 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Apparatus and method for separating air by cryogenic distillation |
US20220252344A1 (en) * | 2019-07-10 | 2022-08-11 | Taiyo Nippon Sanso Corporation | Air separation device and air separation method |
Also Published As
Publication number | Publication date |
---|---|
WO2014102014A2 (de) | 2014-07-03 |
EP2938952A2 (de) | 2015-11-04 |
AU2013369596A1 (en) | 2015-07-02 |
RU2015130628A (ru) | 2017-01-30 |
MX2015008172A (es) | 2015-09-16 |
WO2014102014A3 (de) | 2015-05-28 |
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