WO2016131545A1 - Method and apparatus for obtaining a compressed nitrogen product - Google Patents

Method and apparatus for obtaining a compressed nitrogen product Download PDF

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Publication number
WO2016131545A1
WO2016131545A1 PCT/EP2016/000271 EP2016000271W WO2016131545A1 WO 2016131545 A1 WO2016131545 A1 WO 2016131545A1 EP 2016000271 W EP2016000271 W EP 2016000271W WO 2016131545 A1 WO2016131545 A1 WO 2016131545A1
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WO
WIPO (PCT)
Prior art keywords
pressure column
low
pressure
condenser
heat exchanger
Prior art date
Application number
PCT/EP2016/000271
Other languages
German (de)
French (fr)
Inventor
Dimitri Goloubev
Original Assignee
Linde Aktiengesellschaft
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde Aktiengesellschaft filed Critical Linde Aktiengesellschaft
Priority to US15/548,890 priority Critical patent/US20180023890A1/en
Priority to MX2017010541A priority patent/MX2017010541A/en
Priority to CN201680010982.XA priority patent/CN108207113A/en
Publication of WO2016131545A1 publication Critical patent/WO2016131545A1/en

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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
    • F25J3/04763—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
    • 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
    • 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
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    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
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    • F25J3/0403—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of nitrogen
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    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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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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    • F25J3/04078—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
    • F25J3/04084—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 nitrogen
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    • 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
    • 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
    • F25J3/04763—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
    • F25J3/04896—Details of columns, e.g. internals, inlet/outlet devices
    • F25J3/04915—Combinations of different material exchange elements, e.g. within different columns
    • 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
    • F25J3/04763—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
    • F25J3/04975—Construction and layout of air fractionation equipments, e.g. valves, machines adapted for special use of the air fractionation unit, e.g. transportable devices by truck or small scale use
    • F25J3/04987—Construction and layout of air fractionation equipments, e.g. valves, machines adapted for special use of the air fractionation unit, e.g. transportable devices by truck or small scale use for offshore use
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/94—Details relating to the withdrawal point
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/44—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios

Definitions

  • the invention relates to a method according to the preamble of claim 1.
  • the main condenser and the low-pressure column top condenser are formed in the invention as a condenser-evaporator.
  • the term "condenser-evaporator” refers to a heat exchanger in which a first condensing fluid stream undergoes indirect heat exchange with a second evaporating fluid stream.
  • Each condenser-evaporator has a liquefaction space and a
  • Evaporating passages exist. In the liquefaction space, the condensation (liquefaction) of the first fluid flow is performed, in the evaporation space the evaporation of the second fluid flow. Evaporation and liquefaction space are formed by groups of passages that intercommunicate with each other
  • both capacitors can each be formed by a single heat exchanger block or by a plurality of heat exchanger blocks, which are arranged in a common pressure vessel. Both can be considered one or
  • Falling film evaporator may be formed.
  • the main capacitor can also be used as
  • Heat exchange with recycle streams from the distillation column system can be composed of a single or several parallel and / or serially connected
  • Heat exchanger sections may be formed, for example, from one or more plate heat exchanger blocks.
  • the invention has for its object to provide a method and a corresponding device, which is the recovery of nitrogen flow from the
  • a cold compressor to whose drive the mechanical energy generated in the first residual gas turbine (33) is at least partially used, is here used directly to compress nitrogen product, namely that of the low pressure column, for example, about high pressure column pressure or a higher Pressure is brought.
  • High-pressure column for example, 12 to 17 bar, preferably 13 to 16 bar
  • low pressure column at the top: for example 6 to 10 bar, preferably 7 to 9 bar
  • the first pressurized nitrogen product stream and the second pressurized nitrogen product stream can be heated separately in the main heat exchanger.
  • the first pressurized nitrogen product stream and the second pressurized nitrogen product stream are mixed upstream of the main heat exchanger.
  • an additional third pressure nitrogen stream may be formed by another portion of the nitrogen product of the low pressure column by passing it directly into the main heat exchanger and delivering it as product under the low pressure column pressure (minus pressure drops).
  • the first residual gas turbine and cold compressor are mechanically coupled. This can be accomplished via a common shaft or gear.
  • the residual gas turbine may be mechanically coupled to a generator or an oil brake.
  • the first residual gas turbine is mechanically coupled to an electric generator and the cold compressor is driven by an electric motor; the energy generated in the generator is then electrically transmitted to the engine, thereby driving the cold compressor.
  • Restgases is working expanded in a second residual gas turbine, which is connected in parallel to the first residual gas turbine, which is coupled to the cold compressor.
  • the first residual gas turbine can then be coupled alone with the cold compressor, the second residual gas turbine with a generator or a dissipative brake.
  • Nitrogen compressor are further compressed.
  • both Pressure nitrogen streams are brought together in the nitrogen compressor to a higher pressure.
  • the nitrogen compressor is formed by the ni last stages of the combined n-stage compressor.
  • an eight-stage compressor is used whose three to four last stages as
  • Nitrogen compressor can be used.
  • the invention also relates to a device for obtaining a
  • Figure 1 shows a first embodiment of the invention with a single
  • FIG. 2 shows a second exemplary embodiment with two residual gas turbines
  • FIG. 3 shows a modification of FIG. 1 with a combined compressor
  • FIG. 4 shows a further modification of FIG. 1 with separate heating of the two pressurized nitrogen product streams
  • FIG. 5 shows an embodiment with electrical energy transmission between first residual gas turbine and cold compressor
  • Figure 7 shows an embodiment similar to Figure 6, but with forced-flow evaporators and Figure 8 is a system similar to that of Figure 4, but with columns arranged side by side.
  • atmospheric air is passed through a filter 1 of a
  • Primary air compressor 2 sucked and compressed to a pressure of about 15 bar.
  • the compressed feed air 3 is cooled in a pre-cooler 4. This may include an aftercooler for indirect cooling or a direct contact radiator or both.
  • the pre-cooled feed air 5 is cleaned in a cleaning device 6, which is usually formed by a pair of switchable adsorber.
  • Main heat exchanger 8 cooled to about dew point and via line 9 in the
  • the high-pressure column 10 is part of the distillation column system, which also has a low-pressure column 11, a main condenser 12 and a low-pressure column top condenser 13. A first part 15 of the top gas 14
  • the high-pressure column 10 is introduced into the liquefaction space of the main condenser 12 and condensed there at least partially.
  • Liquid nitrogen 16 formed in the liquefaction space of the main condenser 12 is introduced into the high-pressure column 10 and serves there as a return to a first part.
  • a second part 19 of the top gas 14 of the high-pressure column 10 is the first
  • the warm pressure nitrogen 21 can - as shown in Figure 1 - be further increased in a nitrogen compressor 22 with aftercooler 23 in the pressure, in principle to any desired discharge pressure. It is finally withdrawn as a pressurized nitrogen product (PGAN).
  • the nitrogen compressor 22 and the aftercooler 23 may be omitted.
  • liquid crude oxygen 24 is withdrawn, cooled in the UKG 18 and fed to the low pressure column 11 at an intermediate point.
  • the head gas 26 of the low-pressure column 11 is in the liquefaction of the
  • Liquid nitrogen 27 is introduced into the low-pressure column 11.
  • the bottom liquid 28 of the low-pressure column 11 is cooled in the UKG 18 and via line 29 in the
  • Evaporation space of the low-pressure column head capacitor 13 is introduced, which is purged via a purge line 39 continuously or intermittently.
  • There formed gas is warmed up as residual gas 30 in the UKG 18.
  • the residual gas 31 downstream of the UKGs 18 is supplied to the main heat exchanger 8 at the cold end and heated there to an intermediate temperature.
  • the residual gas 32 under the intermediate temperature is supplied to a first residual gas turbine 33 and there relaxes work.
  • the expanded residual gas 34 is reintroduced into the main heat exchanger 8 and warmed to the warm end.
  • the warmed residual gas 35 leaves the system at about ambient temperature.
  • the residual gas turbine 33 is mechanically coupled to a cold compressor 36 via a common shaft or gear.
  • a nitrogen stream 37 is withdrawn in gaseous form from the top of the low pressure column 11, compressed in the cold compressor 36 to about high pressure column pressure, via a
  • Control valve 41 passed and then mixed as the second pressure nitrogen product stream 38 with the first pressure nitrogen product stream 19 and heated together with this in the main heat exchanger 8 and finally withdrawn as compressed nitrogen product (PGAN).
  • the residual gas turbine 33 does not deliver its entire mechanical energy to the cold compressor 36, but also drives a generator 40, which sits on the same shaft or is connected to the same gear.
  • a dissipative brake may also be used, for example an oil brake.
  • two parallel-connected residual gas turbines 33, 233 are used, one of which is coupled to the cold compressor 36 and the other to a generator 240 (or a dissipative brake).
  • Nitrogen product compressor This allows a PGAN final pressure of about 70 to 100 bar can be achieved.
  • Main heat exchanger 8 warmed up.
  • the warmed nitrogen streams 419 and 438 are combined at 420.
  • the second pressure nitrogen product stream 38 from the cold compressor 36 can thus at a higher temperature in the
  • Main heat exchanger 8 are introduced as the first pressure nitrogen product stream 19.
  • the process can be energetically made slightly cheaper.
  • the electrical energy obtained there is at least partially transmitted via an electrical line network to a motor 540, which in turn is mechanically coupled to the cold compressor 36 and drives it.
  • Figures 2 to 5 can also be combined with each other, for example, to a system with two residual gas turbines and combined compressor and two passage groups in the main heat exchanger for the two pressure nitrogen streams.
  • high-pressure column with sieve trays
  • low-pressure column with packs or sieve trays
  • the invention is also suitable for offshore concepts, such as floating oil recovery plants for oil or gas fields (enhanced oil recovery - EOR).
  • FIG. 6 largely corresponds to FIG. 4, but here additionally a throttle valve 619 is seated in line 419.
  • a modification with a product pressure of 10.9 bar at a high-pressure column pressure of 12.0 bar is shown on the head.
  • Nitrogen flow 37 from the head of the low-pressure column is compressed in the cold compressor 36 here accordingly only to 11, 1 bar, so not quite on the
  • Nitrogen stream 419 from the high pressure column was combined at 420 under the desired pressure of 10.9 bar.
  • the throttling 619 is carried out downstream of the main heat exchanger 8.
  • the throttle losses are surprisingly minimized and the pressure of the feed air can be reduced.
  • the throttling from 12.0 bar to 10.9 bar can also be carried out wholly or partially in the main heat exchanger 8 by a correspondingly high pressure loss is selected there. As a result, the main heat exchanger 8 can be built very compact.
  • FIG. 7 differs from FIG. 6 in that, as the main condenser 12 and the low-pressure column top condenser 13, no bath evaporators but forced-flow evaporators are used. In this case, a purge stream 701 (purge) is withdrawn from the sump of the high-pressure column 10. As the main capacitor 12 may alternatively be used a falling film evaporator.
  • high-pressure column 10 and low-pressure column 11 are not arranged one above the other as in FIGS. 1 to 7, but arranged next to one another. Otherwise, Figure 8 does not differ from Figure 4 or Figure 5 - depending on whether that
  • Nitrogen product is discharged under high-pressure column pressure or under slightly lower pressure (throttle valve 619).

Abstract

The method and apparatus serve to obtain a compressed nitrogen product by low-temperature fractionation of air in a distillation column system having a high-pressure column (10) and a low-pressure column (11) and a main condenser (12) and a low-pressure column top condenser (13), both of which take the form of condenser-evaporators. Bottoms liquid (28, 29) from the low-pressure column is introduced into the evaporation space of the low-pressure column top condenser (13). Gas formed therein is decompressed to perform work as residual gas (30, 31) in a first residual gas turbine (33). The mechanical energy generated is used to drive a cold compressor (36). A first compressed nitrogen product stream (19) is drawn off in gaseous form from the top of the high-pressure column (10) and warmed in the main heat exchanger (8). A further nitrogen stream (37) is drawn off in gaseous form from the top of the low-pressure column (11), compressed in the cold compressor (36) to a pressure which is at least equal to the pressure of the first compressed nitrogen product stream (19) when it is drawn off from the high-pressure column (10), and is then warmed as the second compressed nitrogen product stream (38) in the main heat exchanger (8). The cold compressor (36) overcomes a pressure differential which is at least equal to two thirds of the pressure differential between the top of the high-pressure column (10) and the top of the low-pressure column (11).

Description

Beschreibung  description
Verfahren und Vorrichtung zur Gewinnung eines Druckstickstoffprodukts Process and apparatus for recovering a pressurized nitrogen product
Die Erfindung betrifft ein Verfahren gemäß dem Oberbegriff des Patentanspruchs 1. Die Grundlagen der Tieftemperaturzerlegung von Luft im Allgemeinen sowie derThe invention relates to a method according to the preamble of claim 1. The basics of the cryogenic separation of air in general and the
Aufbau von Zwei-Säulen-Anlagen im Speziellen sind in der Monografie "Tieftemperaturtechnik" von Hausen/Linde (2. Auflage, 1985) und in einem Aufsatz von Latimer in Chemical Engineering Progress (Vol. 63, No.2, 1967, Seite 35) beschrieben. Die Wärmeaustauschbeziehung zwischen Hochdrucksäule und Niederdrucksäule einer Doppelsäule wird im Regelfall durch einen Hauptkondensator realisiert, in dem Construction of two-column plants in particular are described in the monograph "Low Temperature Technique" by Hausen / Linde (2nd edition, 1985) and in an article by Latimer in Chemical Engineering Progress (Vol. 63, No.2, 1967, page 35 ). The heat exchange relationship between high-pressure column and low-pressure column of a double column is usually realized by a main capacitor, in which
Kopfgas der Hochdrucksäule gegen verdampfende Sumpfflüssigkeit der Top gas of the high pressure column against vaporizing bottoms liquid the
Niederdrucksäule verflüssigt wird. Low pressure column is liquefied.
Der Hauptkondensator und der Niederdrucksäulen-Kopfkondensator sind bei der Erfindung als Kondensator-Verdampfer ausgebildet. Als "Kondensator-Verdampfer" wird ein Wärmetauscher bezeichnet, in dem ein erster, kondensierender Fluidstrom in indirekten Wärmeaustausch mit einem zweiten, verdampfenden Fluidstrom tritt. Jeder Kondensator-Verdampfer weist einen Verflüssigungsraum und einen The main condenser and the low-pressure column top condenser are formed in the invention as a condenser-evaporator. The term "condenser-evaporator" refers to a heat exchanger in which a first condensing fluid stream undergoes indirect heat exchange with a second evaporating fluid stream. Each condenser-evaporator has a liquefaction space and a
Verdampfungsraum auf, die aus Verflüssigungspassagen beziehungsweise Evaporation space, which from liquefaction passages respectively
Verdampfungspassagen bestehen. In dem Verflüssigungsraum wird die Kondensation (Verflüssigung) des ersten Fluidstroms durchgeführt, in dem Verdampfungsraum die Verdampfung des zweiten Fluidstroms. Verdampfungs- und Verflüssigungsraum werden durch Gruppen von Passagen gebildet, die untereinander in Evaporating passages exist. In the liquefaction space, the condensation (liquefaction) of the first fluid flow is performed, in the evaporation space the evaporation of the second fluid flow. Evaporation and liquefaction space are formed by groups of passages that intercommunicate with each other
Wärmeaustauschbeziehung stehen. Heat exchange relationship stand.
Dabei können beide Kondensatoren jeweils durch einen einzigen Wärmetauscherblock gebildet werden oder auch durch mehrere Wärmetauscherblöcke, die in einem gemeinsamen Druckbehälter angeordnet sind. Beide können als ein- oder In this case, both capacitors can each be formed by a single heat exchanger block or by a plurality of heat exchanger blocks, which are arranged in a common pressure vessel. Both can be considered one or
mehrstöckige Badverdampfer, Forced-Flow-Verdampfer oder aber als multi-storey bath evaporator, forced-flow evaporator or as
Fallfilmverdampfer ausgebildet sein. Der Hauptkondensator kann außerdem alsFalling film evaporator may be formed. The main capacitor can also be used as
Kaskadenverdampfer ausgestaltet sein, beispielsweise wie in EP 1287302 B1 = US 6748763 B2 beschrieben). Ein "Hauptwärrrietauscher" dient zur Abkühlung von Einsatzluft in indirektem Be configured cascade evaporator, for example, as described in EP 1287302 B1 = US 6748763 B2). A "Hauptwärrrietauscher" is used for cooling of feed air in indirect
Wärmeaustausch mit Rückströmen aus dem Destillationssäulen-System. Er kann aus einem einzelnen oder mehreren parallel und/oder seriell verbundenen Heat exchange with recycle streams from the distillation column system. It can be composed of a single or several parallel and / or serially connected
Wärmetauscherabschnitten gebildet sein, zum Beispiel aus einem oder mehreren Plattenwärmetauscher-Blöcken. Heat exchanger sections may be formed, for example, from one or more plate heat exchanger blocks.
Ein Verfahren der eingangs genannten Art ist aus US 4453957 bekannt. Hier wird die in der Restgasturbine gewonnene mechanische Energie ausschließlich zur A method of the type mentioned is known from US 4453957. Here, the mechanical energy gained in the residual gas turbine is used exclusively for
Kälteerzeugung genutzt. Refrigeration used.
Der Erfindung liegt die Aufgabe zugrunde, ein Verfahren und eine entsprechende Vorrichtung anzugeben, welche die Gewinnung des Stickstoffstroms aus der The invention has for its object to provide a method and a corresponding device, which is the recovery of nitrogen flow from the
Niederdrucksäule unter mindestens Hochdrucksäulendruck erlaubten und dabei einen besonders niedrigeren Energieverbrauch aufweisen. Low pressure column allowed under at least high pressure column pressure and thereby have a particularly low energy consumption.
Diese Aufgabe wird durch die Merkmale des Anspruchs 1 gelöst. This object is solved by the features of claim 1.
Hier wird ein Kaltverdichter, zu dessen Antrieb die in der ersten Restgasturbine (33) erzeugte mechanische Energie mindestens zum Teil genutzt wird, wird hier direkt dazu verwendet, Stickstoffprodukt zu verdichten, und zwar dasjenige der Niederdrucksäule, das beispielsweise auf etwa Hochdrucksäulendruck oder auf einen höheren Druck gebracht wird. Here, a cold compressor, to whose drive the mechanical energy generated in the first residual gas turbine (33) is at least partially used, is here used directly to compress nitrogen product, namely that of the low pressure column, for example, about high pressure column pressure or a higher Pressure is brought.
Im Rahmen der Erfindung hat sich überraschenderweise herausgestellt, dass das erfindungsgemäße Verfahren mit dieser Methode den Niederdrucksäulen-Stickstoff bis auf das Druckniveau des Hochdrucksäulen-Stickstoffs bringt und dabei energetisch günstig ist. Als Nebeneffekt ergibt sich ein relativ einfaches Verfahren und damit auch ein vergleichsweise geringer apparativer Aufwand, insbesondere für den In the context of the invention, it has surprisingly been found that the method according to the invention with this method brings the low-pressure column nitrogen up to the pressure level of the high-pressure column nitrogen and is energetically favorable. As a side effect results in a relatively simple process and thus a comparatively low expenditure on equipment, especially for the
Hauptwärmetauscher. Main heat exchanger.
Bei dem erfindungsgemäßen Verfahren werden die folgenden Druckbereiche verwendet: In the method according to the invention, the following pressure ranges are used:
Hochdrucksäule (am Kopf): beispielsweise 12 bis 17 bar, vorzugsweise 13 bis 16 bar Niederdrucksäule (am Kopf): beispielsweise 6 bis 10 bar, vorzugsweise 7 bis 9 bar Grundsätzlich können bei der Erfindung der erste Druckstickstoffproduktstrom und der zweite Druckstickstoffproduktstrom getrennt im Hauptwärmetauscher angewärmt werden. Vorzugsweise werden jedoch der erste Druckstickstoffproduktstrom und der zweite Druckstickstoffproduktstrom stromaufwärts des Hauptwärmetauschers vermischt. High-pressure column (at the top): for example, 12 to 17 bar, preferably 13 to 16 bar low pressure column (at the top): for example 6 to 10 bar, preferably 7 to 9 bar In principle, in the invention, the first pressurized nitrogen product stream and the second pressurized nitrogen product stream can be heated separately in the main heat exchanger. Preferably, however, the first pressurized nitrogen product stream and the second pressurized nitrogen product stream are mixed upstream of the main heat exchanger.
Bei Bedarf kann ein zusätzlicher dritter Druckstickstoffstrom durch einen anderen Teil des Stickstoffprodukts der Niederdrucksäule gebildet werden, indem dieser direkt in den Hauptwärmetauscher geleitet und unter dem Niederdrucksäulendruck (abzüglich Druckverlusten) als Produkt abgegeben wird. If necessary, an additional third pressure nitrogen stream may be formed by another portion of the nitrogen product of the low pressure column by passing it directly into the main heat exchanger and delivering it as product under the low pressure column pressure (minus pressure drops).
In einer ersten Variante der Energieübertragung zwischen erster Restgasturbine und Kaltverdichter sind die erste Restgasturbine und Kaltverdichter mechanisch gekoppelt. Dies kann über eine gemeinsame Welle oder ein Getriebe bewerkstelligt werden. In a first variant of the energy transfer between the first residual gas turbine and the cold compressor, the first residual gas turbine and cold compressor are mechanically coupled. This can be accomplished via a common shaft or gear.
Für die Erzeugung von Verfahrenskälte kann die Restgasturbine mit einem Generator oder einer Ölbremse mechanisch gekoppelt sein. In einer zweiten Variante der Energieübertragung zwischen erster Restgasturbine und Kaltverdichter ist die erste Restgasturbine an einen elektrischen Generator mechanisch gekoppelt und der Kaltverdichter wird von einem elektrischen Motor angetrieben; die in dem Generator erzeugte Energie wird dann elektrisch auf den Motor übertragen und treibt damit den Kaltverdichter an. For the production of process refrigeration, the residual gas turbine may be mechanically coupled to a generator or an oil brake. In a second variant of the energy transmission between the first residual gas turbine and the cold compressor, the first residual gas turbine is mechanically coupled to an electric generator and the cold compressor is driven by an electric motor; the energy generated in the generator is then electrically transmitted to the engine, thereby driving the cold compressor.
Alternativ kann ein zweiter Teil des auf die Zwischentemperatur angewärmten Alternatively, a second part of the warmed to the intermediate temperature
Restgases in einer zweiten Restgasturbine arbeitsleistend entspannt wird, die der ersten Restgasturbine, die mit dem Kaltverdichter gekoppelt ist, parallelgeschaltet ist. Die erste Restgasturbine kann dann alleine mit dem Kaltverdichter gekoppelt sein, die zweite Restgasturbine mit einem Generator oder einer dissipativen Bremse. Restgases is working expanded in a second residual gas turbine, which is connected in parallel to the first residual gas turbine, which is coupled to the cold compressor. The first residual gas turbine can then be coupled alone with the cold compressor, the second residual gas turbine with a generator or a dissipative brake.
Falls der Druck der Hochdrucksäule nicht ausreicht, können der erste, der zweite oder beide Druckstickstoffströme stromabwärts des Hauptwärmetauschers in einem If the pressure of the high-pressure column is insufficient, the first, second or both pressure nitrogen streams downstream of the main heat exchanger in a
Stickstoffverdichter weiter verdichtet werden. Vorzugsweise werden beide Druckstickstoffströme gemeinsam in dem Stickstoffverdichter auf einen höheren Druck gebracht. Nitrogen compressor are further compressed. Preferably, both Pressure nitrogen streams are brought together in the nitrogen compressor to a higher pressure.
In diesem Fall ist es günstig, die Luftverdichtung und die Stickstoffverdichtung in einer einzigen Maschine zu kombinieren, indem die Einsatzluft in einem Hauptluftverdichter verdichtet wird, der durch die ersten i Stufen eines kombinierten n-stufigen Verdichters gebildet wird, n > 2, i < n. Dabei wird der Stickstoffverdichter durch die n-i letzten Stufen des kombinierten n-stufigen Verdichters gebildet. Beispielsweise wird ein achtstufiger Verdichter verwendet, dessen drei bis vier letzte Stufen als In this case, it is convenient to combine air compression and nitrogen compression in a single engine by compressing the feed air in a main air compressor formed by the first stages of a combined n-stage compressor, n> 2, i <n In this case, the nitrogen compressor is formed by the ni last stages of the combined n-stage compressor. For example, an eight-stage compressor is used whose three to four last stages as
Stickstoffverdichter eingesetzt werden. Nitrogen compressor can be used.
Die Erfindung betrifft außerdem eine Vorrichtung zur Gewinnung eines The invention also relates to a device for obtaining a
Druckstickstoffprodukts durch Tieftemperaturzerlegung von Luft gemäß Pressure nitrogen product by cryogenic separation of air according to
Patentanspruch 14. Claim 14.
Die erfindungsgemäße Vorrichtung kann durch eines, mehrere oder alle Merkmale der unabhängigen Verfahrensansprüche ergänzt werden. The device according to the invention can be supplemented by one, several or all features of the independent method claims.
Die Erfindung sowie weitere Einzelheiten der Erfindung werden im Folgenden anhand von in den Zeichnungen dargestellten Ausführungsbeispielen näher erläutert. Hierbei zeigen: The invention and further details of the invention are explained in more detail below with reference to exemplary embodiments illustrated in the drawings. Hereby show:
Figur 1 ein erstes Ausführungsbeispiel der Erfindung mit einer einzigen Figure 1 shows a first embodiment of the invention with a single
Restgasturbine,  Residual gas turbine,
Figur 2 ein zweites Ausführungsbeispiel mit zwei Restgasturbinen,  FIG. 2 shows a second exemplary embodiment with two residual gas turbines,
Figur 3 eine Abwandlung der Figur 1 mit einem kombinierten Verdichter, Figur 4 eine weitere Abwandlung der Figur 1 mit getrennter Anwärmung der beiden Druckstickstoffproduktströme,  FIG. 3 shows a modification of FIG. 1 with a combined compressor, FIG. 4 shows a further modification of FIG. 1 with separate heating of the two pressurized nitrogen product streams,
Figur 5 eine Ausführungsform mit elektrischer Energieübertragung zwischen erster Restgasturbine und Kaltverdichter,  FIG. 5 shows an embodiment with electrical energy transmission between first residual gas turbine and cold compressor,
Figur 6 eine Abwandlung mit Produktdruck etwas unter dem  Figure 6 shows a modification with product pressure slightly below the
Hochdrucksäulendruck,  High-pressure column pressure,
Figur 7 ein Ausführungsbeispiel ähnlich Figur 6, aber mit Forced-Flow- Verdampfern und Figur 8 ein System ähnlich demjenigen von Figur 4, aber mit nebeneinander angeordneten Säulen. Figure 7 shows an embodiment similar to Figure 6, but with forced-flow evaporators and Figure 8 is a system similar to that of Figure 4, but with columns arranged side by side.
In Figur 1 wird atmosphärische Luft (AIR) durch ein Filter 1 von einem In Fig. 1, atmospheric air (AIR) is passed through a filter 1 of a
Hauptluftverdichter 2 angesaugt und auf einen Druck von ca. 15 bar verdichtet. Die verdichtete Einsatzluft 3 wird in einer Vorkühlungseinrichtung 4 abgekühlt. Diese kann einen Nachkühler zum indirekten Abkühlen oder einen Direktkontaktkühler oder beides enthalten. Die vorgekühlte Einsatzluft 5 wird in einer Reinigungseinrichtung 6 gereinigt, die üblicherweise durch ein Paar umschaltbarer Adsorber gebildet wird. Die Primary air compressor 2 sucked and compressed to a pressure of about 15 bar. The compressed feed air 3 is cooled in a pre-cooler 4. This may include an aftercooler for indirect cooling or a direct contact radiator or both. The pre-cooled feed air 5 is cleaned in a cleaning device 6, which is usually formed by a pair of switchable adsorber. The
verdichtete, vorgekühlte und gereinigte Einsatzluft 7 wird in einem compressed, precooled and purified feed air 7 is in a
Hauptwärmetauscher 8 auf etwa Taupunkt abgekühlt und über Leitung 9 in die  Main heat exchanger 8 cooled to about dew point and via line 9 in the
Hochdrucksäule 10 eingeleitet. High-pressure column 10 initiated.
Die Hochdrucksäule 10 ist Teil des Destillationssäulen-Systems, das außerdem eine Niederdrucksäule 11 , einen Hauptkondensator 12 und einen Niederdrucksäulen- Kopfkondensator 13 aufweist. Ein erster Teil 15 des Kopfgases 14 The high-pressure column 10 is part of the distillation column system, which also has a low-pressure column 11, a main condenser 12 and a low-pressure column top condenser 13. A first part 15 of the top gas 14
der Hochdrucksäule 10 wird in den Verflüssigungsraum des Hauptkondensators 12 eingeleitet und dort mindestens teilweise kondensiert. Im Verflüssigungsraum des Hauptkondensators 12 gebildeter Flüssigstickstoff 16 wird in die Hochdrucksäule 10 eingeleitet und dient dort zu einem ersten Teil als Rücklauf. Zu einem zweiten Teil 17 wird er in einem UKG 18 abgekühlt und auf den Kopf der Niederdrucksäule 11 aufgegeben (49). the high-pressure column 10 is introduced into the liquefaction space of the main condenser 12 and condensed there at least partially. Liquid nitrogen 16 formed in the liquefaction space of the main condenser 12 is introduced into the high-pressure column 10 and serves there as a return to a first part. To a second part 17 it is cooled in a UKG 18 and abandoned on the head of the low-pressure column 11 (49).
Ein zweiter Teil 19 des Kopfgases 14 der Hochdrucksäule 10 wird als erster A second part 19 of the top gas 14 of the high-pressure column 10 is the first
Druckstickstoffproduktstrom 19 über Leitung 20 zum Hauptwärmetauscher 8 geführt und dort auf etwa Umgebungstemperatur angewärmt. Der warme Druckstickstoff 21 kann - wie in Figur 1 dargestellt - in einem Stickstoffverdichter 22 mit Nachkühler 23 weiter im Druck erhöht werden, im Prinzip auf jeden gewünschten Abgabedruck. Er wird schließlich als Druckstickstoffprodukt (PGAN) abgezogen. Für den Fall, dass der gewünschte Produktdruck nicht höher als der Hochdrucksäulendruck (abzüglich der Druckverluste) ist, können der Stickstoffverdichter 22 und der Nachkühler 23 weggelassen werden. Pressure nitrogen product stream 19 passed via line 20 to the main heat exchanger 8 and there warmed to about ambient temperature. The warm pressure nitrogen 21 can - as shown in Figure 1 - be further increased in a nitrogen compressor 22 with aftercooler 23 in the pressure, in principle to any desired discharge pressure. It is finally withdrawn as a pressurized nitrogen product (PGAN). In the case that the desired product pressure is not higher than the high-pressure column pressure (minus the pressure loss), the nitrogen compressor 22 and the aftercooler 23 may be omitted.
Vom Sumpf der Hochdrucksäule 10 wird flüssiger Rohsauerstoff 24 abgezogen, im UKG 18 abgekühlt und der Niederdrucksäule 11 an einer Zwischenstelle zugeleitet. Das Kopfgas 26 der Niederdrucksäule 11 wird in den Verflüssigungsraum des From the bottom of the high pressure column 10 liquid crude oxygen 24 is withdrawn, cooled in the UKG 18 and fed to the low pressure column 11 at an intermediate point. The head gas 26 of the low-pressure column 11 is in the liquefaction of the
Niederdrucksäulen-Kopfkondensators 13 eingeleitet. Der dort gebildete Low-pressure column head capacitor 13 introduced. The educated there
Flüssigstickstoff 27 wird in die Niederdrucksäule 11 eingeleitet. Die Sumpfflüssigkeit 28 der Niederdrucksäule 11 wird im UKG 18 abgekühlt und über Leitung 29 in den Liquid nitrogen 27 is introduced into the low-pressure column 11. The bottom liquid 28 of the low-pressure column 11 is cooled in the UKG 18 and via line 29 in the
Verdampfungsraum des Niederdrucksäulen-Kopfkondensators 13 eingeleitet, der über eine Spülleitung 39 kontinuierlich oder intermittierend gespült wird. Dort gebildetes Gas wird als Restgas 30 wird im UKG 18 angewärmt. Das Restgas 31 stromabwärts des UKGs 18 wird dem Hauptwärmetauscher 8 am kalten Ende zugeführt und dort auf eine Zwischentemperatur angewärmt. Das Restgas 32 unter der Zwischentemperatur wird einer ersten Restgasturbine 33 zugeführt und dort arbeitsleistend entspannt. Das entspannte Restgas 34 wird wieder in den Hauptwärmetauscher 8 eingeführt und bis zum warmen Ende angewärmt. Das angewärmte Restgas 35 verlässt die Anlage unter etwa Umgebungstemperatur. Die Restgasturbine 33 ist über eine gemeinsame Welle oder ein Getriebe mechanisch mit einem Kaltverdichter 36 gekoppelt.  Evaporation space of the low-pressure column head capacitor 13 is introduced, which is purged via a purge line 39 continuously or intermittently. There formed gas is warmed up as residual gas 30 in the UKG 18. The residual gas 31 downstream of the UKGs 18 is supplied to the main heat exchanger 8 at the cold end and heated there to an intermediate temperature. The residual gas 32 under the intermediate temperature is supplied to a first residual gas turbine 33 and there relaxes work. The expanded residual gas 34 is reintroduced into the main heat exchanger 8 and warmed to the warm end. The warmed residual gas 35 leaves the system at about ambient temperature. The residual gas turbine 33 is mechanically coupled to a cold compressor 36 via a common shaft or gear.
Ein Stickstoffstrom 37 wird gasförmig vom Kopf der Niederdrucksäule 11 abgezogen, in dem Kaltverdichter 36 auf etwa Hochdrucksäulendruck verdichtet, über ein A nitrogen stream 37 is withdrawn in gaseous form from the top of the low pressure column 11, compressed in the cold compressor 36 to about high pressure column pressure, via a
Regelventil 41 geleitet und anschließend als zweiter Druckstickstoffproduktstrom 38 mit dem ersten Druckstickstoffproduktstrom 19 vermischt und gemeinsam mit diesem in dem Hauptwärmetauscher 8 angewärmt und schließlich als Druckstickstoffprodukt (PGAN) abgezogen. Control valve 41 passed and then mixed as the second pressure nitrogen product stream 38 with the first pressure nitrogen product stream 19 and heated together with this in the main heat exchanger 8 and finally withdrawn as compressed nitrogen product (PGAN).
Um die Kälteverluste der Anlage zu decken, gibt die Restgasturbine 33 nicht ihre gesamte mechanische Energie an den Kaltverdichter 36 ab, sondern treibt außerdem einen Generator 40 an, der auf der gleichen Welle sitzt beziehungsweise mit dem gleichen Getriebe verbunden ist. Statt des Generators 40 kann auch eine dissipative Bremse verwendet werden, beispielsweise eine Ölbremse. In Figur 2 werden zwei parallel geschaltete Restgasturbinen 33, 233 verwendet, von denen eine an den Kaltverdichter 36 und die andere an einen Generator 240 (oder eine dissipative Bremse) gekoppelt ist. In order to cover the cold losses of the system, the residual gas turbine 33 does not deliver its entire mechanical energy to the cold compressor 36, but also drives a generator 40, which sits on the same shaft or is connected to the same gear. Instead of the generator 40, a dissipative brake may also be used, for example an oil brake. In FIG. 2, two parallel-connected residual gas turbines 33, 233 are used, one of which is coupled to the cold compressor 36 and the other to a generator 240 (or a dissipative brake).
Während in den Figuren 1 und 2 der Hauptluftverdichter 2 und der Stickstoffverdichter 22 durch zwei unabhängige Maschinen gebildet werden, wird in dem Ausführungsbeispiel der Figur 3 ein kombinierter Verdichter 302 eingesetzt, der beide Aufgaben erfüllt. Er weist in dem Ausführungsbeispiel n=8 Stufen auf, von denen i=5 Stufen den Hauptluftverdichter 2 bilden. Die übrigen n-i=3 Stufen bilden den While in FIGS. 1 and 2, the main air compressor 2 and the nitrogen compressor 22 are constituted by two independent machines, FIG Embodiment of Figure 3 is a combined compressor 302 used, which fulfills both tasks. In the exemplary embodiment, it has n = 8 stages, of which i = 5 stages form the main air compressor 2. The remaining ni = 3 stages form the
Stickstoffproduktverdichter. Damit lässt sich ein PGAN-Enddruck von etwa 70 bis 100 bar erreichen. Nitrogen product compressor. This allows a PGAN final pressure of about 70 to 100 bar can be achieved.
In dem Ausführungsbeispiel der Figur 4 werden die beiden In the embodiment of Figure 4, the two
Druckstickstoffproduktströme 19, 38 in getrennten Passagengruppen des Pressurized nitrogen product streams 19, 38 in separate passage groups of the
Hauptwärmetauschers 8 angewärmt. Die angewärmten Stickstoffströme 419 und 438 werden bei 420 zusammengeführt. Der zweite Druckstickstoffproduktstrom 38 aus dem Kaltverdichter 36 kann damit bei einer höheren Temperatur in den Main heat exchanger 8 warmed up. The warmed nitrogen streams 419 and 438 are combined at 420. The second pressure nitrogen product stream 38 from the cold compressor 36 can thus at a higher temperature in the
Hauptwärmetauscher 8 eingeführt werden als der erste Druckstickstoffproduktstrom 19. Damit kann der Prozess energetisch etwas günstiger gestaltet werden. In Figur 5 wird die Energieübertragung zwischen erster Restgasturbine 33 und Main heat exchanger 8 are introduced as the first pressure nitrogen product stream 19. Thus, the process can be energetically made slightly cheaper. In Figure 5, the energy transfer between the first residual gas turbine 33 and
Kaltverdichter 36 im Unterschied zur Figur 1 nicht mechanisch, sondern elektrisch vorgenommen. Dazu ist die erste Restgasturbine 33 mechanisch mit einem Cold compressor 36 in contrast to Figure 1 not mechanically, but made electrically. For this purpose, the first residual gas turbine 33 is mechanically with a
elektrischen Generator 40 gekoppelt. Die dort gewonnene elektrische Energie wird über ein elektrisches Leitungsnetz mindestens teilweise auf einen Motor 540 übertragen, der wiederum mechanisch mit dem Kaltverdichter 36 gekoppelt ist und diesen antreibt. coupled electrical generator 40. The electrical energy obtained there is at least partially transmitted via an electrical line network to a motor 540, which in turn is mechanically coupled to the cold compressor 36 and drives it.
Im Vergleich zu Figur 2 wird das gesamte Restgas in der Generator-Turbine 33/40 entspannt und erzeugt dadurch auch die für den Antrieb des Kaltverdichters Compared to Figure 2, the entire residual gas in the generator turbine 33/40 is relaxed and thus also generates the drive for the cold compressor
notwendige Energie. necessary energy.
Die speziellen Merkmale der Figuren 2 bis 5 können auch untereinander beliebig kombiniert werden, beispielsweise zu einem System mit zwei Restgasturbinen und kombiniertem Verdichter und zwei Passagengruppen im Hauptwärmetauscher für die beiden Druckstickstoffströme. In allen Ausführungsbeispielen sind Hochdrucksäule (mit Siebböden) und Niederdrucksäule (mit Packungen oder Siebböden) übereinander angeordnet. Alternativ können Sie nebeneinander aufgestellt werden. Die Erfindung ist auch für Offshore-Konzepte, beispielsweise für schwimmende (floating) Anlagen zur Gewinnung von Stickstoff für Öl- oder Gasfelder (enhanced oil recovery - EOR) geeignet. Figur 6 entspricht weitgehend Figur 4, allerdings sitzt hier zusätzlich ein Drosselventil 619 in der Leitung 419. Hier wird eine Abwandlung mit einem Produktdruck von 10,9 bar bei einem Hochdrucksäulendruck von 12,0 bar am Kopf gezeigt. Der The special features of Figures 2 to 5 can also be combined with each other, for example, to a system with two residual gas turbines and combined compressor and two passage groups in the main heat exchanger for the two pressure nitrogen streams. In all embodiments, high-pressure column (with sieve trays) and low-pressure column (with packs or sieve trays) are arranged one above the other. Alternatively, they can be placed side by side. The invention is also suitable for offshore concepts, such as floating oil recovery plants for oil or gas fields (enhanced oil recovery - EOR). FIG. 6 largely corresponds to FIG. 4, but here additionally a throttle valve 619 is seated in line 419. Here, a modification with a product pressure of 10.9 bar at a high-pressure column pressure of 12.0 bar is shown on the head. Of the
Stickstoffstrom 37 vom Kopf der Niederdrucksäule wird in dem Kaltverdichter 36 hier entsprechend nur auf 11 ,1 bar verdichtet, also nicht ganz auf den Nitrogen flow 37 from the head of the low-pressure column is compressed in the cold compressor 36 here accordingly only to 11, 1 bar, so not quite on the
Hochdrucksäulendruck. Er wird mit dem im Drosselventil 619 gedrosselten High-pressure column pressure. He is throttled with the throttle valve 619
Stickstoffstrom 419 aus der Hochdrucksäule bei 420 unter dem gewünschten Druck von 10,9 bar vereinigt. Nitrogen stream 419 from the high pressure column was combined at 420 under the desired pressure of 10.9 bar.
Hierbei ist wichtig, dass die Drosselung 619 stromabwärts des Hauptwärmetauschers 8 durchgeführt wird. Damit werden die Drosselverluste überraschend stark minimiert und der Druck der Einsatzluft kann reduziert werden. Die Drosselung von 12,0 bar auf 10,9 bar kann auch ganz oder teilweise im Hauptwärmetauscher 8 durchgeführt werden, indem ein entsprechend hoher Druckverlust dort gewählt wird. Hierdurch kann der Hauptwärmetauscher 8 besonders kompakt gebaut werden. It is important that the throttling 619 is carried out downstream of the main heat exchanger 8. Thus, the throttle losses are surprisingly minimized and the pressure of the feed air can be reduced. The throttling from 12.0 bar to 10.9 bar can also be carried out wholly or partially in the main heat exchanger 8 by a correspondingly high pressure loss is selected there. As a result, the main heat exchanger 8 can be built very compact.
Figur 7 unterscheidet sich dadurch von Figur 6, dass als Hauptkondensator 12 und Niederdrucksäulen-Kopfkondensator 13 keine Badverdampfer, sondern Forced-Flow- Verdampfer eingesetzt werden. In diesem Fall wird ein Spülstrom 701 (Purge) vom Sumpf der Hochdrucksäule 10 abgezogen. Als Hauptkondensator 12 kann alternativ auch ein Fallfilmverdampfer eingesetzt werden. FIG. 7 differs from FIG. 6 in that, as the main condenser 12 and the low-pressure column top condenser 13, no bath evaporators but forced-flow evaporators are used. In this case, a purge stream 701 (purge) is withdrawn from the sump of the high-pressure column 10. As the main capacitor 12 may alternatively be used a falling film evaporator.
In Figur 8 sind Hochdrucksäule 10 und Niederdrucksäule 11 nicht wie in den Figuren 1 bis 7 übereinander, sondern nebeneinander angeordnet. Ansonsten unterscheidet sich Figur 8 nicht von Figur 4 beziehungsweise Figur 5 - je nachdem ob das In FIG. 8, high-pressure column 10 and low-pressure column 11 are not arranged one above the other as in FIGS. 1 to 7, but arranged next to one another. Otherwise, Figure 8 does not differ from Figure 4 or Figure 5 - depending on whether that
Stickstoffprodukt unter Hochdrucksäulendruck oder unter etwas geringerem Druck (Drosselventil 619) abgegeben wird. Nitrogen product is discharged under high-pressure column pressure or under slightly lower pressure (throttle valve 619).

Claims

Patentansprüche claims
Verfahren zur Gewinnung eines Druckstickstoffprodukts durch Process for obtaining a pressure nitrogen product
Tieftemperaturzerlegung von Luft in einem Destillationssäulen-System, das eine Hochdrucksäule (10) und eine Niederdrucksäule (11) sowie einen Cryogenic separation of air in a distillation column system comprising a high pressure column (10) and a low pressure column (11) and a
Hauptkondensator (12) und einen Niederdrucksäulen-Kopfkondensator (13) aufweist, die beide als Kondensator-Verdampfer ausgebildet sind, wobei Main capacitor (12) and a low-pressure column top condenser (13), both of which are formed as a condenser-evaporator, wherein
- verdichtete, vorgekühlte und gereinigte Einsatzluft (7) in einem  - compressed, precooled and cleaned feed air (7) in one
Hauptwärmetauscher (8) abgekühlt und mindestens zum Teil in die  Main heat exchanger (8) cooled and at least partially in the
Hochdrucksäule (10) eingeleitet wird,  High-pressure column (10) is initiated,
- Kopfgas der Hochdrucksäule (14, 15) in den Verflüssigungsraum des  - Top gas of the high pressure column (14, 15) in the liquefaction of the
Hauptkondensators (12) eingeleitet wird und mindestens ein Teil des im Verflüssigungsraum des Hauptkondensators (12) gebildeten Flüssigstickstoffs (16) in die Hochdrucksäule (10) eingeleitet wird,  Main condenser (12) is introduced and at least a portion of the liquid nitrogen (16) formed in the liquefaction space of the main condenser (12) is introduced into the high-pressure column (10),
- Kopfgas (26) der Niederdrucksäule (1 1) in den Verflüssigungsraum des  - Top gas (26) of the low pressure column (1 1) in the liquefaction of the
Niederdrucksäulen-Kopfkondensators (13) eingeleitet wird und mindestens ein Teil des im Verflüssigungsraum des Niederdrucksäulen-Kopfkondensators (13) gebildeten Flüssigstickstoffs (27) in die Niederdrucksäule (11) eingeleitet wird, Low-pressure column head condenser (13) is introduced and at least a portion of the liquid nitrogen (27) formed in the liquefaction space of the low-pressure column overhead condenser (13) is introduced into the low-pressure column (11),
- Sumpfflüssigkeit (28, 29) der Niederdrucksäule (1 1 ) in den Verdampfungsraum des Niederdrucksäulen-Kopfkondensators (13) eingeleitet wird, - bottom liquid (28, 29) of the low-pressure column (1 1) is introduced into the evaporation space of the low-pressure column top condenser (13),
- im Verdampfungsraum des Niederdrucksäulen-Kopfkondensators (13) gebildetes - formed in the evaporation space of the low-pressure column top condenser (13)
Gas als Restgas (30, 31) in dem Hauptwärmetauscher (8) auf eine Gas as residual gas (30, 31) in the main heat exchanger (8) on a
Zwischentemperatur angewärmt, mindestens zu einem ersten Teil (32) in einer ersten Restgasturbine (33) arbeitsleistend entspannt, wieder in den  Warmed intermediate temperature, at least to a first part (32) in a first residual gas turbine (33) work expanded, again in the
Hauptwärmetauscher (8) eingeführt und bis zum warmen Ende des  Main heat exchanger (8) introduced and until the warm end of the
Hauptwärmetauschers (8) angewärmt wird,  Main heat exchanger (8) is warmed up,
ein Stickstoffstrom (37) gasförmig vom Kopf der Niederdrucksäule (11) abgezogen wird und a nitrogen stream (37) is withdrawn in gaseous form from the top of the low-pressure column (11) and
- ein erster Druckstickstoffproduktstrom (19) gasförmig vom Kopf der  a first pressurized nitrogen product stream (19) in gaseous form from the top of the
Hochdrucksäule (10) abgezogen und im Hauptwärmetauscher (8) angewärmt wird,  High pressure column (10) withdrawn and warmed in the main heat exchanger (8),
dadurch gekennzeichnet, dass characterized in that
- die in der ersten Restgasturbine (33) erzeugte mechanische Energie mindestens zum Teil zum Antrieb eines Kaltverdichters (36) verwendet wird - der Stickstoffstrom (37), der gasförmig vom Kopf der Niederdrucksäule (1 1) abgezogen wurde, in dem Kaltverdichter (36) auf einen Druck verdichtet wird, der mindestens gleich dem Druck des ersten Druckstickstoffproduktstroms (19) beim Abziehen aus der Hochdrucksäule (10) minus 2 bar ist, und anschließend als zweiter Druckstickstoffproduktstrom (38) in dem Hauptwärmetauscher (8) angewärmt wird und - The mechanical energy generated in the first residual gas turbine (33) is at least partially used to drive a cold compressor (36) - The nitrogen stream (37), which was withdrawn in gaseous form from the head of the low pressure column (1 1) is compressed in the cold compressor (36) to a pressure which is at least equal to the pressure of the first pressure nitrogen product stream (19) when removing from the high pressure column (10 ) is minus 2 bar, and then as the second pressure nitrogen product stream (38) in the main heat exchanger (8) is warmed and
- der Stickstoffstrom (37), der gasförmig vom Kopf der Niederdrucksäule (11)  - the nitrogen stream (37), which is gaseous from the top of the low-pressure column (11)
abgezogen wurde, in dem Kaltverdichter (36) auf einen Druck verdichtet wird, der mindestens gleich dem Druck des ersten Druckstickstoffproduktstroms (19) beim Abziehen aus der Hochdrucksäule (10) minus 2 bar ist, und anschließend als zweiter Druckstickstoffproduktstrom (38) in dem Hauptwärmetauscher (8) angewärmt wird, wobei  wherein the cold compressor (36) is compressed to a pressure which is at least equal to the pressure of the first pressurized nitrogen product stream (19) when withdrawn from the high pressure column (10) minus 2 bar, and then as the second pressurized nitrogen product stream (38) in the main heat exchanger (8) is warmed, wherein
- der Kaltverdichter (36) eine Druckdifferenz überwindet, die mindestens gleich zwei Dritteln der Druckdifferenz zwischen Kopf der Hochdrucksäule (10) und Kopf der Niederdrucksäule (1 ) ist.  - The cold compressor (36) overcomes a pressure difference which is at least equal to two thirds of the pressure difference between the head of the high pressure column (10) and the head of the low pressure column (1).
2. Verfahren nach Anspruch 1 , dadurch gekennzeichnet, dass der erste 2. The method according to claim 1, characterized in that the first
Druckstickstoffproduktstrom (19) und der zweite Druckstickstoffproduktstrom (38) stromaufwärts des Hauptwärmetauschers (8) vermischt werden.  Pressurized nitrogen product stream (19) and the second pressurized nitrogen product stream (38) are mixed upstream of the main heat exchanger (8).
3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass die erste 3. The method according to claim 1 or 2, characterized in that the first
Restgasturbine (33) mit dem Kaltverdichter (36) über eine gemeinsame Welle oder ein Getriebe mechanisch gekoppelt ist.  Restgasturbine (33) is mechanically coupled to the cold compressor (36) via a common shaft or a transmission.
4. Verfahren nach Anspruch 3, dadurch gekennzeichnet, dass die erste 4. The method according to claim 3, characterized in that the first
Restgasturbine (33) außerdem mit einem elektrischen Generator (40) oder einer Ölbremse mechanisch gekoppelt ist.  Restgas turbine (33) is also mechanically coupled to an electric generator (40) or an oil brake.
5. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass die erste 5. The method according to claim 1 or 2, characterized in that the first
Restgasturbine (33) an einen elektrischen Generator (40) mechanisch gekoppelt ist, der Kaltverdichter (36) von einem elektrischen Motor (540) angetrieben wird und die in dem Generator (40) erzeugte Energie mindestens teilweise elektrisch auf den Motor (540) übertragen wird. Residual gas turbine (33) is mechanically coupled to an electric generator (40), the cold compressor (36) by an electric motor (540) is driven and the energy generated in the generator (40) is at least partially electrically transmitted to the motor (540) ,
6. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass ein zweiter Teil des auf die Zwischentemperatur angewärmten Restgases (32) in einer zweiten Restgasturbine (233) arbeitsleistend entspannt wird, die der ersten Restgasturbine (33) parallel geschaltet ist. 6. The method according to any one of claims 1 to 5, characterized in that a second part of the warmed to the intermediate temperature residual gas (32) in a second residual gas turbine (233) is working expanded, which is connected in parallel to the first residual gas turbine (33).
7. Verfahren nach Anspruch 6, dadurch gekennzeichnet, dass erste Restgasturbine (33) mit dem Kaltverdichter (36) und die zweite Restgasturbine mit einem 7. The method according to claim 6, characterized in that first residual gas turbine (33) with the cold compressor (36) and the second residual gas turbine with a
Generator (240) oder einer dissipativen Bremse mechanisch gekoppelt ist.  Generator (240) or a dissipative brake is mechanically coupled.
8. Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, dass der erste, der zweite oder beide Druckstickstoffströme stromabwärts des 8. The method according to any one of claims 1 to 7, characterized in that the first, the second or both pressure nitrogen streams downstream of the
Hauptwärmetauschers (8) in einem Stickstoffverdichter (22) weiter verdichtet werden.  Main heat exchanger (8) in a nitrogen compressor (22) are further compressed.
9. Verfahren nach Anspruch 8 dadurch gekennzeichnet, dass die Einsatzluft in einem Hauptluftverdichter (2) verdichtet wird, der durch die ersten i Stufen eines kombinierten n-stufigen Verdichters (302) gebildet wird, n > 2, i < n, und dass der Stickstoffverdichter (22) durch die n-i letzten Stufen des kombinierten n-stufigen Verdichters (302) gebildet wird. 9. The method according to claim 8, characterized in that the feed air is compressed in a main air compressor (2), which is formed by the first i stages of a combined n-stage compressor (302), n> 2, i <n, and that Nitrogen compressor (22) is formed by the ni last stages of the combined n-stage compressor (302).
10. Verfahren nach einem der Ansprüche 1 bis 9, dadurch gekennzeichnet, dass der Stickstoffstrom (37), der gasförmig vom Kopf der Niederdrucksäule (11) abgezogen wurde, in dem Kaltverdichter (36) auf einen Druck verdichtet wird, der mindestens gleich dem Druck des ersten Druckstickstoffproduktstroms (19) beim Abziehen aus der Hochdrucksäule (10) ist. 10. The method according to any one of claims 1 to 9, characterized in that the nitrogen stream (37), which was withdrawn in gaseous form from the head of the low-pressure column (11) is compressed in the cold compressor (36) to a pressure which is at least equal to the pressure of the first pressurized nitrogen product stream (19) when withdrawn from the high pressure column (10).
11. Verfahren nach einem der Ansprüche 1 bis 10, dadurch gekennzeichnet, dass der erste Druckstickstoffproduktstrom (19) und der zweite Druckstickstoffproduktstrom (38) in getrennten Passagen angewärmt und insbesondere anschließend vereinigt werden. 11. The method according to any one of claims 1 to 10, characterized in that the first pressurized nitrogen product stream (19) and the second pressurized nitrogen product stream (38) are warmed in separate passages and in particular subsequently combined.
12. Verfahren nach einem der Ansprüche 1 bis 11 , dadurch gekennzeichnet, dass mindestens eine, mehrere oder alle der folgenden Maßnahmen angewendet werden: 12. The method according to any one of claims 1 to 11, characterized in that at least one, several or all of the following measures are applied:
- Ausbildung des Hauptkondensators (12) als Forced-Flow-Verdampfer, - Ausbildung des Hauptkondensators (12) als Fallfilmverdampfer,Formation of the main condenser (12) as a forced flow evaporator, Formation of the main condenser (12) as a falling-film evaporator,
- Ausbildung des Niederdrucksäulen-Kopfkondensators (13) als Forced-Flow-- Formation of the low-pressure column top condenser (13) as a forced flow
Verdampfer. Evaporator.
13. Verfahren nach einem der Ansprüche 1 bis 12, dadurch gekennzeichnet, dass13. The method according to any one of claims 1 to 12, characterized in that
- die Niederdrucksäule (11) neben der Hochdrucksäule (10), the low-pressure column (11) next to the high-pressure column (10),
- der Hauptkondensator (12) über der Hochdrucksäule (10) und  - The main condenser (12) above the high pressure column (10) and
- der Niederdrucksäulen-Kopfkondensator (13) über der Niederdrucksäule angeordnet sind.  - The low-pressure column top condenser (13) are arranged above the low-pressure column.
14. Vorrichtung zur Gewinnung eines Druckstickstoffprodukts durch 14. Apparatus for recovering a pressure nitrogen product by
Tieftemperaturzerlegung von Luft mit  Cryogenic decomposition of air with
- einem Destillationssäulen-System, das eine Hochdrucksäule (10) und eine  a distillation column system comprising a high pressure column (10) and a
Niederdrucksäule (11) sowie einen Hauptkondensator (12) und einen  Low pressure column (11) and a main capacitor (12) and a
Niederdrucksäulen-Kopfkondensator (13) aufweist, die beide als Kondensator- Verdampfer ausgebildet sind, mit  Low-pressure column top condenser (13), which are both formed as a condenser evaporator, with
- einem Hauptwärmetauscher (8) zum Abkühlen verdichteter, vorgekühlter und gereinigter Einsatzluft (7) wobei  - A main heat exchanger (8) for cooling compressed, precooled and purified feed air (7) wherein
- der Verflüssigungsraum des Hauptkondensators (12) mit dem Kopf der  - The liquefaction space of the main capacitor (12) with the head of
Hochdrucksäule (10) in Strömungsverbindung (14, 15, 16) steht,  High pressure column (10) in flow communication (14, 15, 16),
- der Verflüssigungsraum des Niederdrucksäulen-Kopfkondensators (13) mit dem - The liquefaction space of the low-pressure column top condenser (13) with the
Kopf der Niederdrucksäule (11) in Strömungsverbindung (26, 27) steht, und der Verdampfungsraum des Niederdrucksäulen-Kopfkondensators (13) mit dem Sumpf der Niederdrucksäule (11) in Strömungsverbindung (28, 29) steht, und mit Head of the low-pressure column (11) in flow communication (26, 27) is, and the evaporation space of the low-pressure column head condenser (13) with the bottom of the low-pressure column (11) in flow communication (28, 29) is in fluid communication (28, 29)
- Mitteln zum Entnehmen von im Verdampfungsraum des Niederdrucksäulen- - means for removing in the evaporation chamber of Niederdrucksäulen-
Kopfkondensators (13) gebildetem Gas als Restgas (30, 31), Top condenser (13) formed gas as residual gas (30, 31),
- Mitteln zum Anwärmen des Restgases (31) in dem Hauptwärmetauscher (8) auf eine Zwischentemperatur,  Means for heating the residual gas (31) in the main heat exchanger (8) to an intermediate temperature,
- einer ersten Restgasturbine (33) zum arbeitsleistenden Entspannen des  - A first residual gas turbine (33) for work-relaxing of the
teilangewärmten Restgases (32),  partially heated residual gases (32),
- Mitteln zum Einleiten des entspannten Restgases (34) in den  - Means for introducing the expanded residual gas (34) in the
Hauptwärmetauscher (8) und Mitteln zum Entnehmen des angewärmten Restgases vom warmen Ende des Hauptwärmetauschers (8), - Mitteln zum Verwenden von in der ersten Restgasturbine (33) erzeugter mechanischer Energie zum Antrieb eines Kaltverdichters (36) und Main heat exchanger (8) and means for removing the warmed residual gas from the warm end of the main heat exchanger (8), - means for using in the first residual gas turbine (33) generated mechanical energy for driving a cold compressor (36) and
- einer ersten Druckstickstoffproduktleitung zum Abziehen eines gasförmigen ersten Druckstickstoffproduktstroms (19) vom Kopf der Hochdrucksäule (10) und zum Anwärmen des ersten Druckstickstoffproduktstroms (19) im  a first pressurized nitrogen product line for withdrawing a gaseous first pressurized nitrogen product stream (19) from the head of the high pressure column (10) and for heating the first pressurized nitrogen product stream (19) in the
Hauptwärmetauscher (8),  Main heat exchanger (8),
gekennzeichnet durch marked by
- Mittel zum Abziehen eines gasförmigen Stickstoffstroms (37) vom Kopf der - means for removing a gaseous nitrogen stream (37) from the top of the
Niederdrucksäule (1 ), Low-pressure column (1),
- Mittel zum Einleiten des gasförmigen Stickstoffstroms (37) in den Kaltverdichter - Means for introducing the gaseous nitrogen stream (37) in the cold compressor
(36) und (36) and
- Mittel zum Einleiten des kaltverdichteten Stickstoffstroms als zweiter  - Means for introducing the cold-compressed nitrogen stream as the second
Druckstickstoffproduktstrom (38) in dem Hauptwärmetauscher (8),  Pressurized nitrogen product stream (38) in the main heat exchanger (8),
- wobei der Kaltverdichter (36) dazu ausgebildet ist, eine Druckdifferenz zu  - Wherein the cold compressor (36) is adapted to a pressure difference
überwinden, die mindestens gleich zwei Dritteln der Druckdifferenz zwischen Kopf der Hochdrucksäule (10) und Kopf der Niederdrucksäule (11) ist.  overcome, which is at least equal to two thirds of the pressure difference between the head of the high pressure column (10) and the head of the low pressure column (11).
PCT/EP2016/000271 2015-02-19 2016-02-18 Method and apparatus for obtaining a compressed nitrogen product WO2016131545A1 (en)

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