EP1413840A1 - Procédé et dispositif de production variable d'oxygen par séparation cryogénique d'air - Google Patents

Procédé et dispositif de production variable d'oxygen par séparation cryogénique d'air Download PDF

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Publication number
EP1413840A1
EP1413840A1 EP03002838A EP03002838A EP1413840A1 EP 1413840 A1 EP1413840 A1 EP 1413840A1 EP 03002838 A EP03002838 A EP 03002838A EP 03002838 A EP03002838 A EP 03002838A EP 1413840 A1 EP1413840 A1 EP 1413840A1
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European Patent Office
Prior art keywords
oxygen
pressure
liquid
nitrogen
pressure column
Prior art date
Legal status (The legal status 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 status listed.)
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EP03002838A
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German (de)
English (en)
Inventor
Gerhard Pompl
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Linde GmbH
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Linde GmbH
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—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
    • 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
    • F25J3/04436—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system
    • F25J3/04442—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system in a double column flowsheet with a high pressure pre-rectifier
    • 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
    • F25J3/04436—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system
    • F25J3/04448—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system in a double column flowsheet with an intermediate pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04472—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • F25J3/04503—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
    • F25J3/04509—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems within the cold part of the air fractionation, i.e. exchanging "cold" within the fractionation and/or main heat exchange line
    • 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
    • F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/50—Processes or apparatus involving steps for increasing the pressure of gaseous 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
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams

Definitions

  • the invention relates to a method for the variable generation of oxygen by low-temperature decomposition of air, in which feed air is introduced into a distillation column system which comprises at least one medium-pressure column and a low-pressure column, in the distillation column system generates a liquid oxygen fraction and at least is temporarily introduced into an oxygen tank, a liquid nitrogen fraction is generated in the distillation column system and is at least temporarily introduced into a nitrogen tank and in which, when there is an increased demand for oxygen, liquid oxygen is removed from the oxygen tank, evaporated by indirect heat exchange and obtained as a gaseous oxygen product.
  • the object of the invention is to further increase the flexibility of such a method.
  • the distillation column system also has a high-pressure column which operates under higher pressure than the medium-pressure column is and into which at least part of the feed air is introduced, and that in the indirect heat exchange to evaporate the liquid oxygen from the oxygen tank, a nitrogen-rich fraction from the high-pressure column is liquefied.
  • the flexibility of oxygen production can be increased considerably, particularly with regard to product pressure.
  • the pressure during the evaporation of the oxygen is no longer tied to the operating pressure of the low pressure column, but can be set independently of this with the help of a corresponding selection of the operating pressure of the high pressure column.
  • This evaporation produces a nitrogen-rich liquid which can be used in the distillation column system to improve the separation performance.
  • any fraction from the high-pressure column whose nitrogen content is greater than that of the air can be used as the heating medium (“nitrogen-rich fraction”) for evaporating the liquid oxygen.
  • the top gas of the high pressure column is preferably used.
  • the pressure of the liquid oxygen from the oxygen tank is increased upstream of its evaporation.
  • This enables a higher product pressure to be achieved in the oxygen gas.
  • the air introduced into the high pressure column must have a pressure that is higher than the operating pressure of the medium pressure column.
  • either the total air can be compressed to the high pressure or - to save energy - the air flow that forms the insert of the high pressure column can be compressed accordingly.
  • the nitrogen-rich liquid fraction which arises during the evaporation of the liquid oxygen is preferably at least partially introduced into one or more columns of the distillation column system and used there as reflux.
  • nitrogen gas from the high-pressure column is expanded while performing work in the process according to the invention.
  • This can be, for example trade a gas which has the same composition and the same origin as the above-mentioned nitrogen-rich fraction.
  • the amount of nitrogen gas which is relaxed during work is varied with the oxygen requirement. In this way, the cold production can be adapted to the respective operating situation.
  • the exact pattern of the control of a nitrogen turbine depending on the oxygen requirement is explained in detail in the Rohde article cited above and is used analogously in the method of the invention.
  • the combination of pressure evaporation and external compression can be used in particular for automatic control of the system depending on the oxygen demand (pipeline following) by measuring the pressure in the product line (pipeline) behind the gas compressor and the amount of gaseous oxygen product flowing through the gas compressor depending is set by this pressure.
  • the invention also relates to a device for the low-temperature separation of air according to claim 7.
  • a first partial flow 2 flows under this pressure to the cold end of a main heat exchanger 3, where it is cooled to about dew point and then introduced into a medium pressure column 6 via line 4 without pressure-changing measures.
  • the medium pressure column 6 is part of a distillation column system which also has a high pressure column 5 and a low pressure column 6, as well as two condenser evaporators, a top condenser 8 of the high pressure column and a top condenser 9 of the medium pressure column.
  • the two condenser evaporators 8, 9 are designed as falling film evaporators.
  • one or each of both can be designed as a circulation evaporator [thermosiphon evaporator].
  • the medium pressure column 6, the top condenser (main condenser) 9 and the low pressure column 7 are analogous to connected to a conventional Linde double column.
  • the spatial arrangement shown in the drawing is not essential to the invention; for example, the three components could also be arranged one above the other.
  • liquid raw oxygen is obtained and is introduced into the low-pressure column 7 via line 10, supercooling counterflow 11, line 12 and throttle valve 13.
  • Gaseous top nitrogen 14 of the medium pressure column 6 is practically completely liquefied in the top condenser 9.
  • the condensate 15 formed here is fed to a first part 16 as a return to the medium pressure column 6.
  • the rest is drawn off via line 17, supercooled (in FIG. 11) and fed via line 18 and throttle valve 19 into a separator (phase separator) 20 which is at approximately the same pressure as the low-pressure column 7.
  • the liquid Nitrogen 21 flows via line 22 to the top of the low pressure column and optionally via line 23 to a nitrogen tank 24. Flash gas is withdrawn via line 25.
  • gaseous nitrogen 26 leaves the low-pressure column and flows together with the flash gas 25 from the separator 20 via line 27, supercooling counterflow 11 and line 28 to the cold end of the main heat exchanger 3.
  • the nitrogen 29 is converted into a gaseous product ( GAN) deducted.
  • the oxygen product 30 is removed from the bottom of the low-pressure column 7 in liquid form, brought to an increased pressure in a pump 31 and introduced to a first part 32-33 into the evaporation chamber of the top condenser 9 of the medium-pressure column 6.
  • Another part of the pumped liquid oxygen optionally flows via lines 34 and 35 through subcooling countercurrent 11 into an oxygen tank 36.
  • a second partial flow 37 of the compressed and cleaned feed air 1 is further compressed in a post-compressor 38 with after-cooler 39.
  • the high pressure air 40 is cooled in the main heat exchanger 3 and fed into the high pressure column 5 via line 41. This is operated at a higher pressure than the medium pressure column 6.
  • Crude oxygen 42 from the sump of the high pressure column 5 is transferred to the medium pressure column 6 via a throttle valve 43.
  • Part of gaseous top nitrogen 44 of the high pressure column 5 is almost completely liquefied in the top condenser 8.
  • the condensate 46 formed here is fed to a first part 47 as a return to the high-pressure column 5.
  • the rest is drawn off via line 48, supercooled (in FIG.
  • the top condenser 8 of the high-pressure column 5 is cooled with a further part 60 of the liquid oxygen 30 pumped in 31 from the low-pressure column 7.
  • the pressure at the outlet of the pump 31 is set such that the oxygen 60 in the condenser 8 evaporates from the high-pressure column 5 against the condensing nitrogen.
  • the vaporized oxygen 61 is supplied to the main heat exchanger 3 at least to a first part 62 under the increased pressure and is heated there to approximately ambient temperature.
  • the warm oxygen 63-64 can be further compressed in a gas compressor (oxygen compressor) 65 to the desired product pressure or drawn off via line 66.
  • the rest Gaseous oxygen 67 is introduced together with that from the top condenser 9 of the medium-pressure column 6 into the lower region of the low-pressure column 7, where it serves as rising steam.
  • Another part 51 of the gaseous top nitrogen 44 of the high-pressure column 5 is heated to an intermediate temperature in the main heat exchanger 3. At this intermediate temperature, it flows via line 52 to an expansion machine (nitrogen turbine) 53 and is expanded there while performing work, which is braked by means of a generator 54. The expanded nitrogen 55 is finally mixed with the nitrogen product 28 drawn off from the low-pressure column 7.
  • an expansion machine nitrogen turbine
  • the two liquid tanks 24, 36 and the nitrogen turbine 53 perform the same function as described in detail in the Rohde article mentioned above, namely to compensate for fluctuations in the oxygen demand while the columns of the distillation column system are being loaded by buffering liquid.
  • FIG. 1 also shows the measuring and control devices that are required for carrying out the alternate storage.
  • the corresponding Control systems (symbolized by broken lines in the drawing) are generally integrated in an integrated digital control system.
  • the total amount of air to be separated is measured in line 1 (FIC - Flow Indication and Control 73) and set on the main air compressor (MAC - Main Air Compressor), not shown.
  • the distribution of the air volume between the first and second partial streams 2, 37 is measured in line 40 (FIC 74) and can be changed by adjusting the guide blades of the post-compressor 38.
  • the liquid balance of the columns is monitored by liquid level measuring devices (LIC - Liquid Indication and Control 75, 76, 77). For example, if the liquid level in the respective column sump increases, the discharge 42, 10 - 12-13 or 30 - 34 - 35 of oxygen-enriched liquid is increased (valves 43, 13, 56 for high-pressure column, medium-pressure column or low-pressure column) and / or the feed 57 , 59 of liquid oxygen 59 reduced in the low pressure column (by opening the valve 78). Concentration measurements (AIC - Analysis Indication and Control 79, 50) at medium height of the high pressure column and medium pressure column determine the return flow requirement.
  • LIC - Liquid Indication and Control 75, 76, 77 liquid level measuring devices
  • the throughput through valve 19 or 50 and / or the throughput through valve 84 is reduced.
  • the return flow for the low pressure column is kept constant (FIC 81).
  • Liquid level controller 82 acts on valve 83 and ensures that excess liquid nitrogen flows into tank 24.
  • the pressure upstream and downstream of the oxygen compressor 65 is measured (85, 86), and the total amount of the oxygen product (87).
  • the corresponding actuating devices act on the guide vanes of the oxygen compressor 65 and on valve 88.
  • the flow through the nitrogen turbine 52 is measured (93) and adjusted by means of the guide vanes of this turbine (94).
  • These measuring and control devices enable automatic control of the system depending on the oxygen demand (pipeline following) at increased pressure in the gaseous oxygen product.
  • the pipeline pressure drops, which the operations control system registers through the pressure measurement 86.
  • the flow control increases the throughput through compressor 65.
  • the Nitrogen turbine 53 is retracted, which increases the conversion at the top condenser 8 of the high-pressure column, as a result of which the additionally required oxygen is evaporated.
  • the liquid level controllers 75, 76, 77 and the analysis measurements 79, 80 ensure that the operation of the columns remains constant by adding missing or excess liquids from the buffer tanks 24, 36 or draining them there. If the compressor is at its swallowing limit and the pipeline pressure is still falling, the setpoint of the suction pressure regulator is automatically increased and the compressor throughput is increased. If the demand for oxygen drops, the control proceeds in the opposite direction.
  • the oxygen discharge pressure downstream of the gas compressor 65 can be varied as necessary.
  • Figure 2 largely corresponds to Figure 1. Only the differences are described below.
  • the second exemplary embodiment has a third partial flow 289 of the feed air, which is compressed together with the second partial flow 41 in the post-compressor 38. However, it is led out of the main heat exchanger 3 at an intermediate temperature and fed to a second expansion machine (air turbine) 290, where it relaxes to perform the pressure of the medium pressure column 6, for example. The mechanical energy generated in this way is transmitted to an electrical generator 291.
  • the third partial flow 292, which has been relieved of work, is fed with the cooled first partial flow 4 via line 204 into the medium-pressure column 6. In this way, additional cold can be obtained, which can be used to produce liquid products, which are preferably drawn off from one or both liquid tanks 24, 36 (not shown). Optimizing the inlet temperatures of the two turbines also improves the heat transfer in the main heat exchanger.

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  • Physics & Mathematics (AREA)
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EP03002838A 2002-10-23 2003-02-07 Procédé et dispositif de production variable d'oxygen par séparation cryogénique d'air Withdrawn EP1413840A1 (fr)

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DE10249383 2002-10-23
DE2002149383 DE10249383A1 (de) 2002-10-23 2002-10-23 Verfahren und Vorrichtung zur variablen Erzeugung von Sauerstoff durch Tieftemperatur-Zerlegung von Luft

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2573492A1 (fr) * 2011-09-20 2013-03-27 Linde Aktiengesellschaft Procédé et dispositif destinés à la décomposition à basse température d'air
WO2013041229A1 (fr) * 2011-09-20 2013-03-28 Linde Aktiengesellschaft Procédé et dispositif de séparation cryogénique de l'air
CN106288657A (zh) * 2016-10-21 2017-01-04 成都深冷液化设备股份有限公司 液氧、液氮互换生产装置及生产工艺
US10852061B2 (en) 2017-05-16 2020-12-01 Terrence J. Ebert Apparatus and process for liquefying gases
EP3889529A1 (fr) * 2020-04-02 2021-10-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Dispositif de réglage de la quantité d'alimentation en gaz produit et appareil de séparation d'air le comprenant

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR102260840B1 (ko) * 2020-02-25 2021-06-07 주식회사 케이씨 가스 공급 시스템

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US4604116A (en) * 1982-09-13 1986-08-05 Erickson Donald C High pressure oxygen pumped LOX rectifier
US5084081A (en) * 1989-04-27 1992-01-28 Linde Aktiengesellschaft Low temperature air fractionation accommodating variable oxygen demand
EP0524785A1 (fr) * 1991-07-23 1993-01-27 The Boc Group, Inc. Séparation d'air
US5471843A (en) * 1993-06-18 1995-12-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of oxygen and/or nitrogen under pressure at variable flow rate
US5656557A (en) * 1993-04-22 1997-08-12 Nippon Sanso Corporation Process for producing various gases for semiconductor production factories
US5953937A (en) * 1995-07-21 1999-09-21 Linde Aktiengesellschaft Process and apparatus for the variable production of a gaseous pressurized product
US6185960B1 (en) * 1998-04-08 2001-02-13 Linde Aktiengesellschaft Process and device for the production of a pressurized gaseous product by low-temperature separation of air
WO2002101216A1 (fr) * 2001-06-08 2002-12-19 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et installation de production d'energie au moyen d'une turbine a gaz associee a une entite de separation d'air

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4604116A (en) * 1982-09-13 1986-08-05 Erickson Donald C High pressure oxygen pumped LOX rectifier
US5084081A (en) * 1989-04-27 1992-01-28 Linde Aktiengesellschaft Low temperature air fractionation accommodating variable oxygen demand
EP0524785A1 (fr) * 1991-07-23 1993-01-27 The Boc Group, Inc. Séparation d'air
US5656557A (en) * 1993-04-22 1997-08-12 Nippon Sanso Corporation Process for producing various gases for semiconductor production factories
US5471843A (en) * 1993-06-18 1995-12-05 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of oxygen and/or nitrogen under pressure at variable flow rate
US5953937A (en) * 1995-07-21 1999-09-21 Linde Aktiengesellschaft Process and apparatus for the variable production of a gaseous pressurized product
US6185960B1 (en) * 1998-04-08 2001-02-13 Linde Aktiengesellschaft Process and device for the production of a pressurized gaseous product by low-temperature separation of air
WO2002101216A1 (fr) * 2001-06-08 2002-12-19 L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede et installation de production d'energie au moyen d'une turbine a gaz associee a une entite de separation d'air

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2573492A1 (fr) * 2011-09-20 2013-03-27 Linde Aktiengesellschaft Procédé et dispositif destinés à la décomposition à basse température d'air
WO2013041229A1 (fr) * 2011-09-20 2013-03-28 Linde Aktiengesellschaft Procédé et dispositif de séparation cryogénique de l'air
AU2012311959B2 (en) * 2011-09-20 2016-09-08 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
US10443931B2 (en) 2011-09-20 2019-10-15 Linde Aktiengesellschaft Method and device for the cryogenic decomposition of air
CN106288657A (zh) * 2016-10-21 2017-01-04 成都深冷液化设备股份有限公司 液氧、液氮互换生产装置及生产工艺
CN106288657B (zh) * 2016-10-21 2019-04-12 成都深冷液化设备股份有限公司 液氧、液氮互换生产装置及生产工艺
US10852061B2 (en) 2017-05-16 2020-12-01 Terrence J. Ebert Apparatus and process for liquefying gases
EP3889529A1 (fr) * 2020-04-02 2021-10-06 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Dispositif de réglage de la quantité d'alimentation en gaz produit et appareil de séparation d'air le comprenant

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