US20160161181A1 - Method and device for producing compressed nitrogen - Google Patents

Method and device for producing compressed nitrogen Download PDF

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Publication number
US20160161181A1
US20160161181A1 US14/906,162 US201414906162A US2016161181A1 US 20160161181 A1 US20160161181 A1 US 20160161181A1 US 201414906162 A US201414906162 A US 201414906162A US 2016161181 A1 US2016161181 A1 US 2016161181A1
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pressure
stream
pressure column
substream
low
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Alexander Alekseev
Dimitri Goloubev
Thomas Eckert
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Linde GmbH
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Linde GmbH
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Assigned to LINDE AKTIENGESELLSCHAFT reassignment LINDE AKTIENGESELLSCHAFT ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: GOLOUBEV, DIMITRI, ECKERT, THOMAS, ALEKSEEV, ALEXANDER
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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
    • 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
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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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
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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
    • F25J3/04521—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
    • F25J3/04569—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for enhanced or tertiary oil recovery
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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
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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
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    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
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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
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    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04787—Heat exchange, e.g. main heat exchange line; Subcooler, external reboiler-condenser
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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
    • F25J3/04763—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.
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—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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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/52—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the high pressure column of a double pressure main column system
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
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    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/52—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen enriched compared to air ("crude 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

Definitions

  • the invention relates to a method of producing compressed nitrogen according to the preamble of claim 1 .
  • the pressure figures here generally do not include the natural pressure drops. Pressures here are regarded as “equal” when the pressure difference between appropriate points is not greater than the natural conduction losses which are caused by pressure drops in pipelines, heat exchangers; coolers, adsorbers, etc.
  • the internal compression nitrogen stream experiences a pressure drop in the passages of the main heat exchanger; nevertheless, the release pressure of the compressed nitrogen product downstream of the main heat exchanger and the pressure upstream of the main heat exchanger are referred to here equally as “the product pressure”.
  • a “condenser-evaporator” refers so a heat exchanger in which a first condensing fluid scream enters into indirect heat exchange with a second evaporating fluid stream, every condenser-evaporator has a liquefaction space and an evaporation space consisting respectively of liquefaction passages and evaporation passages.
  • the condensation (liquefaction) of a first fluid stream is conducted, and in the evaporation space the evaporation of a second fluid stream.
  • the evaporation and liquefaction spaces are formed by groups of passages in a heat-exchanging relationship with one another.
  • the “main heat exchanger” serves to cool feed air in indirect heat exchange with return streams from the distillation column system, it may be formed from a single heat exchanger section or a plurality of heat exchanger sections connected in parallel and/or in series, for example from one or more plate heat exchanger blocks.
  • the main heat exchanger in this context is formed, for example, in U.S. 6,141,989 by the combination of a gas-gas exchanger with a condenser-evaporator in which pumped high-pressure column nitrogen is evaporated in indirect heat exchange with a condensing substream of the feed air.
  • the “internal compression nitrogen stream” is evaporated against a high-pressure air stream (or pseudo-evaporated if its pressure is supercritical) and warmed. At the same time, the high-pressure air is cooled and liquefied or, if its pressure is supercritical, pseudo-liquefied.
  • the high-pressure air is cooled and liquefied or, if its pressure is supercritical, pseudo-liquefied.
  • no separate condenser-evaporator is used for nitrogen evaporation; instead, the (pseudo-) evaporation and the warming take place in an integrated main heat exchanger.
  • oxygen-enriched product gas stream is understood here to mean any gaseous product stream or residual stream which is released by the system and has an oxygen content higher than that of air. This may be very pure oxygen or else an only slightly oxygen-enriched residual gas.
  • the process of the invention may have one or more streams of this kind.
  • the known process thus requires two externally driven compressors 3 and 5 , as shown in schematic form in FIG. 1 , in order to provide a compressed nitrogen product under more than 12 bar.
  • Air fractionation in the narrower sense 7 is represented by a conventional air fractionation plant which produces mid-pressure nitrogen (PGAN—pressurized gaseous nitrogen) under a pressure of, for example, 12 bar.
  • This mid-pressure nitrogen then has to be compressed further in a nitrogen gas compressor 5 to a pressure of, for example, 100 bar in order to be able to release it as high-pressure nitrogen (HPGAN—high pressure gaseous nitrogen), for example to promote mineral oil production (to EOR—enhanced oil recovery).
  • GPN mid-pressure nitrogen
  • HPGAN high pressure gaseous nitrogen
  • the apparatus complexity can also be kept comparatively low by using only a single externally driven compressor in spite of the high air pressure, namely the main air compressor.
  • This of course does not rule out single-stage turbine-driven compressors (boosters) which do not require any external energy but are effectively driven by the energy generated in the main air compressor, which is converted to mechanical energy in the work-performing decompression in the turbine.
  • the “first substream” which is decompressed to perform work is formed by the overall remainder of the overall air stream which is not required as “second substream” for the internal compression.
  • the “first substream” of the air can be cooled before the work-performing decompress ion to below ambient temperature, especially in she main heat exchanger to an intermediate temperature between the temperatures of the warm and cold ends of the main heat exchanger. It then enters the work-performing decompression in the caseous state and is ultimately introduced at least partly in the gaseous state into the distillation column system, especially into the high-pressure column.
  • the gas content of the first substream forms the ascending vapor in the lower region of the high-pressure column.
  • the first substream decompressed to perform work can be partly or fully liquefied in a reboiler of the high-pressure column and fed in liquid form into the high-pressure column; the ascending gas in the lower region of the high-pressure column is then formed by the vapor generated in the high-pressure column reboiler.
  • distillation column system is thus not operated like a conventional Linde double column (in other words, the high-pressure column top condenser is not cooled by bottoms liquid from the low-pressure column); instead, the high-pressure column top condenser is operated with exclusively with liquid air (i.e. with a liquid having the same or a similar composition to atmospheric air).
  • the “second portion of the feed air” is introduced, directly or via a separator (phase separator) which may be disposed in a separate vessel, or incorporated into the high-pressure column, into the evaporation space of the high-pressure column top condenser, without previously being involved in the rectification in any of the columns in the distillation column system.
  • a separator phase separator
  • the two columns may be arranged alongside one another without any need for process pumps for raising liquids. This makes the system more compact and allows the columns to be substantially prefabricated and then transported to the erection site.
  • the maim air compressor has a single drive unit which is formed especially by a gas turbine unit, a steam turbine, a gas engine or a diesel engine.
  • this drive unit is the sole source of external energy in the entire system apart from liquid pumps which consume very much less energy than gas compressors, and apart from the energy supply for auxiliary devices such as regulation and control units, lighting, etc.
  • This achieves a very substantial simplification of the compressor drive; generators, transformers and electric motors for the gas compression are unnecessary and hence cannot contribute to energy losses. This is especially true when the main air compressor is the sole external energy-driven gas compressor which is used in the method.
  • the second substream of the high-pressure overall air stream is decompressed and hence liquefied in a decompression turbine (fluid turbine) rather than being decompressed in a throttle valve, and is then introduced into the distillation column system.
  • a decompression turbine fluid turbine
  • a “third substream” of the first liquid nitrogen stream is applied as reflux to the low-pressure column, and the internal compression nitrogen stream is formed by a second substream of the second liquid nitrogen stream.
  • the expression “third substream” means here that a “second substream” of the first liquid nitrogen stream may but need not exist in the method.
  • the internal compression nitrogen stream is formed by a second substream of the first liquid nitrogen stream (from the high-pressure column top condenser) and a second substream of the second liquid nitrogen stream (from the low-pressure column top condenser), these two substreams being brought to the product pressure separately.
  • nitrogen is being consumed under two or more different product pressures, it is also possible in a modified embodiment to bring the two second substreams to different product pressures or to decompress substreams to the pressures required (after pumping); the different internal compression nitrogen streams under the different pressures are then conducted separately through the main heat exchanger and obtained as compressed nitrogen products under different pressures.
  • the second substream of the second liquid nitrogen stream (from the low-pressure column top condenser) is first brought to about high-pressure column pressure in the liquid state, and then combined with the second substream of the first liquid nitrogen stream (from the high-pressure column top condenser) to the.
  • the mixture then constitutes the internal compression nitrogen stream and is brought collectively from the high-pressure column pressure to the product pressure in a further step.
  • Cooling energy in the method of the invention is preferably generated in a single decompression machine, with at least partial introduction of the first substream of the high-pressure overall air stream, downstream of the work-performing decompression thereof, into the high-pressure column.
  • the decompression machine may be formed, for example, by an expansion turbine. It may be coupled to a recompressor in which the first substream of the high-pressure overall air stream downstream of the work-performing decompression thereof or the second substream of the high-pressure overall air stream or the high-pressure overall air stream is recompressed to a pressure higher than the overall air pressure.
  • the method of the invention needs just two condenser-evaporators: the high-pressure column top condenser and the low-pressure column top condenser. In specific cases, however, it may be favorable to use a third condenser evaporator in the form of a high-pressure column reboiler.
  • Bottoms liquid from the high-pressure column is evaporated therein in indirect heat exchange with condensing air which is introduced in the form of a third portion of the high-pressure overall air stream into the liquefaction space of the high-pressure column reboiler.
  • the evaporated bottoms liquid is introduced into the high-pressure column as ascending gas and enhances the separating action therein.
  • the “third portion” of the high-pressure overall air stream can be formed by the first substream which has been decompressed to perform work or by a portion thereof.
  • energy can be saved by recompressing the second substream of the air in a turbine-driven recompressor to a second air pressure higher than the overall air pressure.
  • the recompressor (booster) is preferably driven by the decompression machine in which the first substream of the air is decompressed so perform work.
  • the second substream ( 52 ) of the high-pressure overall air stream ( 11 , 811 ) is decompressed and hence liquefied in a decompression turbine (rather than the decompression in a throttle valve) and then introduced into the distillation column system.
  • This decompression turbine (fluid turbine) is preferably attenuated by a generator which generates electrical energy.
  • the energy efficiency in the method of the invention can be further improved by a booster circuit for the high-pressure column (claim 12 ) or a booster circuit for the low-pressure column (claim 13 ) or by a combination of these two booster circuits.
  • the invention also relates to an apparatus according to claim 14 .
  • the apparatus of the invention can be supplemented by apparatus features corresponding to the features of the dependent method claims.
  • FIGS. 2 to 12 show:
  • FIG. 2 the operation of an air fractionation plant of the invention with a gas turbine unit as the sole drive
  • FIGS. 3 to 5 three embodiments of the distillation column system of a system of the invention
  • FIGS. 6 and 7 two embodiments of a cooling and liquefaction unit of a system of the invention.
  • FIGS. 8 and 9 two embodiments of air pretreatment and cooling and liquefaction units of a system of the invention
  • FIG. 10 one working example of the method of the invention in overview.
  • FIGS. 11 and 12 two further working examples of the invention with booster circuits.
  • FIG. 2 shows part of the air fractionation plant downstream of the main air compressor 9 , merely in schematic form as box 10 (ASU).
  • ASU air pretreatment unit
  • cooling and liquefaction unit and a distillation column system.
  • atmospheric air In the main air compressor 9 having several stages with intermediate cooling, atmospheric air (AIR) is compressed to an overall air pressure which is higher than 20 bar and in a specific numerical example is 37.5 bar.
  • the high-pressure overall air stream 11 HP-AIR which exits the main air compressor 9 is introduced into the air fractionation plant in the narrower sense 10 .
  • an internally compressed nitrogen product stream 12 ICGAN—internally compressed gaseous nitrogen
  • the nitrogen product stream 12 is used in the use example to promote mineral oil production (to EOR—enhanced oil recovery).
  • Ail stages of the main air compressor are driven by means of a common, shaft connected to the shaft of a gas turbine unit 1 which a gas turbine compressor 13 , a gas turbine combustion chamber 14 , a gas turbine expander 15 and—optionally—a steam raising unit 16 (HRSG—heat recovery steam generation).
  • the gas turbine compressor 13 compresses ambient air (amb); the combustion chamber 14 burns natural gas (NG) with the compressed air. Heat is withdrawn from the combustion gas from the combustion chamber 14 in the steam-raising; the cold combustion gas—optionally after cleaning—is blown back into the ambient environment (amb).
  • FIG. 3 shows a first working example of a distillation column system as used in the invention.
  • the distillation column system has a high-pressure column 202 with high-pressure column top condenser 204 and a low-pressure column 203 with low-pressure column top condenser 205 .
  • Both top condensers take the form of condenser-evaporators.
  • the operating pressures of the columns (at the top in each case) in the example are
  • the gaseous component from line 208 ascends within the high-pressure column 202 ; the liquid component is at least partly withdrawn again and introduced via line 210 and throttle valve 211 into the evaporation space of the high-pressure column top condenser 204 , as is a further liquid air stream 221 which is formed by the small amount of liquid generated in the work-performing decompression. Vapor generated in the evaporation space of the high-pressure column top condenser 204 is drawn off via line 212 and fed to the lower region of the low-pressure column 203 as ascending vapor.
  • Gaseous top nitrogen 213 from the high-pressure column 202 is introduced at least in a first portion 214 into the liquefaction space of the high-pressure column top condenser 204 and liquefied at least partly therein, preferably completely or almost completely.
  • a first substream 216 of the first liquid nitrogen stream 215 is applied as reflux liquid to the high-pressure column 202 .
  • Another portion (the “third substream”) 217 of the first liquid nitrogen stream 215 is cooled in a subcooling countercurrent heat exchanger 218 and, after throttle expansion 219 , fed via line 220 into the low-pressure column 203 . (In the working example of FIG. 3 , there is no “second substream” of the first liquid nitrogen stream 215 .)
  • the oxygen-enriched bottoms liquid 222 from the high-pressure column 202 is subcooled in the subcooling countercurrent heat exchanger 218 and introduced via throttle valve 223 and line 224 into the evaporation space of the low-pressure column top condenser 205 .
  • a further cooling fluid for the low-pressure column top condenser 205 is formed by the cooling liquid 225 of the low-pressure column 203 which, is likewise subcooled in the subcooling countercurrent heat exchanger 218 , throttled ( 226 ) and introduced ( 227 ) into the evaporation space of the low-pressure column top condenser 205 .
  • purge liquid 228 from the high-pressure column top condenser 204 is introduced into the evaporation space of the low-pressure column top condenser 205 .
  • a purge liquid is likewise drawn off from the evaporation space of the low-pressure column top condenser 205 and discarded or compressed to the supercritical pressure and passed through the main heat exchanger.
  • At least a first portion 231 of the gaseous top nitrogen 230 from the low-pressure column 203 is liquefied at least partly, preferably completely or almost completely. This forms a second liquid nitrogen stream 232 .
  • a first substream 233 of the second liquid nitrogen stream 232 is applied as further reflux liquid to the low-pressure column 203 .
  • a second substream 234 is fed to an internal compression and brought therein in a pump 235 in the liquid state to a product pressure which is between 20 and 100 bar and in the example is about 70 bar.
  • the supercritical nitrogen ICLIN—internally compressed liquid nitrogen
  • Vapor formed in the low-pressure column top condenser 205 is drawn off via line 240 , warmed in the subcooling countercurrent heat exchanger 218 and finally fed as residual gas (WASTE) to the cooling and liquefaction unit.
  • WASTE residual gas
  • a portion of the gaseous top nitrogen from the high-pressure column 202 or the low-pressure column 203 can be obtained directly as gaseous pressure product (HPGAN—high pressure gaseous nitrogen/MPGAH—medium pressure gaseous nitrogen), which is of course warmed up to about ambient temperature in the cooling and liquefaction unit.
  • HPGAN high pressure gaseous nitrogen/MPGAH—medium pressure gaseous nitrogen
  • LIN liquid nitrogen product
  • a separate separator can be used; in that case, the gaseous component is introduced into the high-pressure column, and the liquid component at least partly into the evaporation space of the high-pressure column top condenser 204 .
  • FIG. 4 While only a single internal compression pump 235 is used in FIG. 3 , two of them are used in FIG. 4 .
  • a first pump 335 a brings the second substream 334 of the second liquid nitrogen stream 232 , as in FIG. 3 , from the low-pressure column pressure to the product pressure; in contrast to FIG. 3 , however, this stream comprises not the entire internally compressed product but only a portion.
  • the remainder of the internally compressed, nitrogen is formed by a second substream 319 of the first liquid nitrogen stream 215 , which is brought from the high-pressure column pressure to the product pressure in a second pump 335 b.
  • the two internal compression nitrogen streams are combined at 337 and together form the supercritical nitrogen (ICLIN) in line 336 .
  • ICLIN supercritical nitrogen
  • a portion 343 of the liquid air from the cup 209 is cooled in the subcooling counter current heat exchanger 318 and fed via line 344 to the low-pressure column 203 at an intermediate point.
  • FIG. 5 differs from FIG. 4 by a third condenser-evaporator: the high-pressure column reboiler 438 .
  • the gaseous air 401 AIR
  • the liquid 442 formed is additionally introduced into the cup 209 .
  • FIGS. 5 and 7 show two embodiments of a cooling and liquefaction unit 50 which can be combined with FIG. 2 and any of the distillation column systems of FIGS. 3 to 6 .
  • the entire cleaned high-pressure overall air stream 811 (see FIGS. 8 and 9 ) is fed under the overall air pressure to the warm end of a main heat exchanger 51 implemented here as a single plate heat exchanger block.
  • a first substream 56 of the high-pressure overall air stream 811 is withdrawn from the main heat exchanger at a first intermediate temperature and fed to an expansion turbine 57 which drives a recompressor 53 .
  • the air 58 decompressed to perform work is introduced into a separator (phase separator) 59 .
  • the majority of the first substream 58 decompressed to perform work is introduced via line 201 in gaseous form into the high-pressure column of the distillation column system; the liquid 221 removed is treated as described in FIG. 3 .
  • a second substream 52 of the high-pressure overall air stream 811 is withdrawn again at a second, higher intermediate temperature and recompressed to about 50 bar in the turbine-driven recompressor (booster) 53 with recooler 54 .
  • the recompressed second substream 55 is introduced back into the warm end of the main heat exchanger 51 , conducted down to the cold end therein and pseudo-liquefied therein.
  • the supercritical second substream 206 is introduced into the distillation column system in the manner shown in FIGS. 3 to 6 .
  • the supercritical internal compression nitrogen 236 / 336 flows under the product pressure to the cold end of the main heat exchanger 31 . It is pseudo-evaporated therein and warmed to an out ambient temperature and finally obtained in gaseous form as internally compressed nitrogen product 60 (ICGAN).
  • the gaseous streams 237 , 238 and 241 from the distillation column system are also warmed to about ambient temperature in the main heat exchanger 51 .
  • the warmed nitrogen streams are released as products 61 / 62 (HPGAN/MPGAN).
  • the warmed residual gas stream is partly blown off into the ambient environment (amb) via line 63 and partly used as regeneration gas in the cleaning unit 802 for the feed air (see FIGS. 8 and 9 ).
  • the high-pressure column 202 and low-pressure column 203 arranged alongside one another. If a particularly small footprint is available, however, it is also possible in the invention to arrange the columns one on top of another similarly to a conventional Linde double column. In this case, beginning from the bottom, the following apparatus parts are positioned in a line one on top of another:
  • high-pressure column 202 (in the case of FIG. 5 with a high-pressure column reboiler 438 incorporated into the high-pressure column)
  • FIG. 7 differs by the line 765 from FIG. 6 .
  • the second substream 752 of the high-pressure overall air stream is not precooled here in the main heat exchanger but by the admixing of a small portion 765 of the cold first substream 756 before entry into the turbine 57 .
  • FIG. 8 shows, as well as the cooling and liquefaction unit 50 from FIG. 6 , a first embodiment of an air pretreatment unit 799 .
  • the compressor stages 804 , 806 and 807 and the coolers 805 and 808 of the main air compressor 9 are not part of the air pretreatment unit.
  • the compressed overall air 800 is cooled to about ambient temperature in a pre coo ling unit 801 and then cleaned in a cleaning unit 802 having molecular sieve adsorbers.
  • the cleaned high-pressure overall air stream 811 compressed to the overall air pressure is introduced into the cooling and liquefaction unit 50 .
  • the air pretreatment unit 799 can be operated under the overall air pressure (see FIG. 10 ). Given the high air pressures used here, however, it is more favorable in most cases to operate the air pretreatment unit as shown in FIG. 8 under a lower pressure, by arranging it between two stages 806 and 807 of the main air compressor. This makes the design of molecular sieve adsorber vessels and switching valves simpler and lowers the losses on changeover of the adsorbers.
  • All three stages 804 , 806 and 807 of the main air compressor 9 of the working example are driven by a single shaft connected to the shaft of a gas turbine unit, a gas engine or another engine. Between the first two stages 804 and 806 is disposed an intermediate cooler 805 , and beyond the third and last stage a
  • FIG. 9 differs from FIG. 8 in that a portion 902 of the supercritical high-pressure air 901 is not conducted via line 206 to the distillation column system but decompressed in a throttle valve 903 to an intermediate pressure corresponding to the inlet pressure of the last stage 807 of the main air compressor 9 (plus conduction losses). It is warmed fully in the main heat exchanger 51 and then fed to the inlet of the last stage 807 of the main air compressor 9 . This increases the amount of high-pressure air used for evaporation of internal compression nitrogen. This leads to a reduction in the final pressure of the main air compressor, and it is possible to reduce the number of compressor stages (cost advantage).
  • FIG. 10 shows a working example of the method of the invention in its entirety, here, the precooling unit 801 and the cleaning unit 802 of the air pretreatment unit 799 are operated under the overall air pressure.
  • the main air compressor 9 has multiple stages with intermediate cooling and is formed by a single machine.
  • the shaft thereof is driven by an electric motor, si steam turbine, a gas turbine unit, a gas engine or another engine, for example a diesel engine.
  • the cooling and liquefaction unit 50 shown in FIG. 10 corresponds to that of FIG. 6 , and the distillation column system 1000 to that of FIG. 3 .
  • the air pretreatment unit 799 and the main air compressor 9 of FIG. 10 can be combined with any of the other cooling and liquefaction units described here and with any of the other distillation column systems described in this application.
  • FIG. 11 The working example of FIG. 11 is based on FIG. 10 . It has a fluid turbine (dense fluid turbine) 1107 rather than the throttle valve 207 and is also equipped with a booster circuit.
  • a fluid turbine discharge fluid turbine 1107 rather than the throttle valve 207 and is also equipped with a booster circuit.
  • Vapor drawn off from the evaporation apace of the high-pressure column top condenser 204 is fed here only in a portion 1112 to the low-pressure column 203 .
  • the remainder forms a circulation stream 1172 which is compressed in a one-stage compressor (booster) 1173 , which takes the form of a cold compressor, from about 3.9 bar to about 6.9 bar.
  • the compressed circulation stream 1174 is introduced into the main heat exchanger 51 at an intermediate point and cooled therein up to the cold end.
  • the cold circulation stream 1175 is fed back to the high-pressure column 202 at the bottom and boosts the separation process therein. Therefore, the whole circuit is referred, to as a booster circuit.
  • the work-performing decompression of the first substream 56 of the high-pressure overall air stream 11 is conducted in two parallel-connected expansion turbines 57 a, 57 b.
  • the first turbine 57 a drives the warm recompressor 53 for the first substream 752 , and the second turbine 57 b the cold compressor 1173 .
  • the two turbines 57 a, 57 b in the working example have the same inlet, and outlet parameters in terms of pressure and temperature (in other working examples, the inlet temperatures may also be different).
  • FIG. 12 differs from FIG. 11 in that the booster circuit 1272 / 1273 / 1274 / 1275 leads not from the evaporation space of the high-pressure column top condenser into the high-pressure column but from the top of the low-pressure column 203 into the liquefaction space of the high-pressure column top condenser 204 .
  • This increases the conversion in the high-pressure column top condenser 204 and hence the amount of ascending gas 212 for the low-pressure column 203 , i.e. the conversion in the low-pressure column.
  • FIG. 11 it is also possible in the methods of FIGS. 11 and 12 to additionally draw off gaseous nitrogen product directly from the top of the high-pressure column 202 and/or of the low-pressure column 203 and warm it in the main heat exchanger 51 .
  • the booster circuits shown in FIG. 11 and FIG. 12 can be combined with any of the other cooling and liquefaction units described here and with any of the other distillation column systems described in this application.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US14/906,162 2013-08-02 2014-07-29 Method and device for producing compressed nitrogen Abandoned US20160161181A1 (en)

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EP13003861 2013-08-02
EP13003861.5 2013-08-02
PCT/EP2014/002074 WO2015014485A2 (de) 2013-08-02 2014-07-29 Verfahren und vorrichtung zur erzeugung von druckstickstoff

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WO2022179748A1 (de) * 2021-02-25 2022-09-01 Linde Gmbh Verfahren und anlage zur bereitstellung von druckstickstoff

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