WO2007068858A2 - Process for separating air by cryogenic distillation - Google Patents
Process for separating air by cryogenic distillation Download PDFInfo
- Publication number
- WO2007068858A2 WO2007068858A2 PCT/FR2006/051350 FR2006051350W WO2007068858A2 WO 2007068858 A2 WO2007068858 A2 WO 2007068858A2 FR 2006051350 W FR2006051350 W FR 2006051350W WO 2007068858 A2 WO2007068858 A2 WO 2007068858A2
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- WO
- WIPO (PCT)
- Prior art keywords
- oxygen
- flow
- air
- column
- pressure
- Prior art date
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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
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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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
- C01B13/02—Preparation of oxygen
- C01B13/0229—Purification or separation processes
- C01B13/0248—Physical processing only
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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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- 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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- 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
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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
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
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- 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
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- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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- 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
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- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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- 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
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- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
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- 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
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- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
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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
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- F25J3/0446—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 heat generated by mixing two different phases
- F25J3/04466—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 heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid oxygen
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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
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- 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
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- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J3/04763—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
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
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- C01B2210/00—Purification or separation of specific gases
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- C—CHEMISTRY; METALLURGY
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- C—CHEMISTRY; METALLURGY
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- C01B2210/00—Purification or separation of specific gases
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
- F25J2215/54—Oxygen production with multiple pressure O2
-
- 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
- F25J2230/24—Multiple compressors or compressor stages 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- 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
- F25J2240/42—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 air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
Definitions
- the present invention relates to a process for air separation by cryogenic distillation, in particular to a method and installation for supplying oxygen at two pressures and / or two purities.
- a steel production unit typically comprises several elements with different oxygen requirements, as described in "The Making, Shaping and Treating of Steel", AISE, 1985.
- the blast furnace consumes air enriched with oxygen, usually produced by mixing compressed air with medium pressure oxygen (P ⁇ 10 bar) and in some cases low purity.
- the low purity oxygen has a purity of between 80 and 97%.
- Converters and arc furnaces consume oxygen at high pressure (P> 15 bar for injection into a converter, and P> 25 bar typically in the gas buffer capacities installed upstream of the converters) with a high purity of between 99 and 99.8%.
- high pressure P> 15 bar for injection into a converter, and P> 25 bar typically in the gas buffer capacities installed upstream of the converters
- P> 15 bar for injection into a converter
- P> 25 bar typically in the gas buffer capacities installed upstream of the converters
- high purity of between 99 and 99.8% a high purity of between 99 and 99.8%.
- it is often provided two devices for producing oxygen by air distillation the one that produces the medium pressure oxygen being for example a mixing column apparatus of the type described in US-A. 4022030 and EP-A-0531 182 and the one producing the high purity oxygen typically being a conventional double column apparatus. All the purities mentioned are molar percentages and the pressures are absolute pressures.
- the present invention aims to solve the following problem: sometimes the customer has increased needs for high pressure oxygen while he no longer needs medium pressure oxygen (or no longer needs as much oxygen) medium pressure / or can operate with a reduced (or even zero) amount of medium pressure oxygen [as is the case for the blast furnace]).
- the object of the invention is to satisfy the customer without resorting to either a second air separation apparatus or to the vaporization of cryogenic liquid oxygen from storage.
- a method for separating air by cryogenic distillation in an air separation apparatus comprising a column system in which i) according to a first step a) is compressed in a main compressor all the air intended for distillation b) a first compressed air flow is sent at least in the main compressor, purified and cooled in an exchange line to the medium pressure column of a double column c) separating the air flow in flows enriched in nitrogen and oxygen in the medium pressure column d) the nitrogen and oxygen enriched streams of the medium pressure column are sent to a low pressure column of the double column, directly or indirectly e) a flow rich in nitrogen is withdrawn from the low pressure column and is heated in the exchange line f) a liquid oxygen flow rate is withdrawn from the low pressure column, pressurized to a high pressure e and vaporized in the exchange line to form a first gaseous flow rich in oxygen and at high pressure g) liquefies at least a portion of the compressed air in the main compressor, optionally after recompress
- the second gaseous flow rich in oxygen is produced by withdrawing a liquid flow from the low pressure column and pressurizing it at the lower pressure before vaporizing it in the exchange line;
- the second gas flow rich in oxygen is produced by withdrawing a gas flow from a mixing column supplied with air or the low pressure column; the at least one second compressor compresses all the air intended for the apparatus;
- the at least one second compressor compresses only a portion of the air intended for the apparatus
- a portion of the compressed air in the second compressor is expanded in a turbine coupled to the second compressor and sent to the double column and in which the flow expanded during the second step reduced compared to that during the first step; during the second step, the flow rate sent to the second compressor with respect to the same flow rate during the first step is kept constant;
- the first flow rich in oxygen has a purity higher than 98.5%, and the second flow rich in oxygen has a purity lower than 98%; -
- the first step is withdrawn from the double column as a final product oxygen-rich liquid flow and in the second step the withdrawal of this flow is reduced, possibly to zero;
- the sum of the first and second oxygen-rich flow rates is substantially constant between the first and second steps;
- a flow of air is expanded in a turbine and sent to the double column and during the second step is the expanded flow is rejected to the atmosphere or a part of the expanded flow is sent to the double column while the rest is rejected to the atmosphere; during the second step, compressed air is sent to the double column coming from a backup compressor;
- the first and second oxygen-rich flow rates have the same purity or different purities.
- a method for supplying a high pressure oxygen flow rate wherein in a first step each of two air separation plants supplies high pressure oxygen and according to a second step, a first of the two facilities provides an increased high pressure oxygen flow compared to that in the first step and the second installation provides a reduced flow, or even zero; at least the first plant operating as described above and providing in addition to its initial production of high pressure oxygen at least 50% of the amount of high pressure oxygen produced during the first step by the second installation.
- an air compressor of the second installation sends compressed air to the first installation during the second step
- FIG. 1 A schematic diagram of a typical air separation apparatus.
- FIG. 1 A schematic diagram of a typical air separation apparatus.
- FIG. 1 A schematic diagram of a typical air separation apparatus.
- FIG. 1 A schematic diagram of a typical air separation apparatus.
- FIG. 1 A schematic diagram of a typical air separation apparatus.
- FIG. 1 A schematic diagram of a typical air separation apparatus.
- FIG. 1 A schematic diagram of a typical air separation apparatus.
- FIG. 1 The air distillation plant shown in FIG.
- an air compressor 1 essentially comprises: an air compressor 1, an apparatus 2 for cleaning compressed air with water and adsorption CO 2 , this apparatus comprising two bottles of adsorption 2A, 2B, one of which operates in adsorption while the other is being regenerated, a turbine-booster assembly 3 comprising an expansion turbine 4, and optionally a booster 5 whose shaft is coupled to that of the turbine 4, a heat exchanger 6 constituting the heat exchange line of the installation, a double distillation column 7 comprising a medium pressure column 8 surmounted by a low pressure column 9, with a vaporizer-condenser 10 setting the steam head (nitrogen) of the column 8 in heat exchange relation with the tank liquid (oxygen) of the column 9, a liquid oxygen tank 11 whose bottom is connected to a liquid oxygen pump 12, and a reservoir of liquid nitrogen 13 whose bottom is connected to a liquid nitrogen pump 14.
- This installation is intended to supply, via a pipe 15, gaseous oxygen under a predetermined high pressure, which may be between a few bars and a few tens of bars (in this specification, the pressures considered are absolute pressures).
- liquid oxygen withdrawn from the tank of the column 9 via a pipe 16 and stored in the tank 11, is brought to the high pressure by the pump 12 in the liquid state, then vaporized and heated under this high pressure in passages 17 of the exchanger 8.
- the heat required for this vaporization and reheating, as well as the reheating and possibly the vaporization of other fluids withdrawn from the double column, is provided by the air to be distilled under the following conditions.
- All of the air to be distilled is compressed by the compressor 1 at a pressure higher than the average pressure of the column 8 but lower than the high pressure of oxygen. Then the air, pre-cooled at 18 and cooled to near room temperature at 19, is purified in one, 2A for example, adsorption bottles, and supercharged entirely at high pressure by the booster 5, which is driven by the turbine 4.
- the air is then introduced to the hot end of the exchanger 6 and completely cooled to an intermediate temperature. At this temperature, a fraction of the air continues cooling and is liquefied in passages 20 of the exchanger, then is expanded at low pressure in an expansion valve 21 and introduced at an intermediate level in column 9. The the remainder of the air, or excess air, is expanded at the medium pressure in the turbine 4 and then sent directly, via a pipe 22, to the base of the column 8.
- the low pressure nitrogen is heated in passages 28 of the exchanger 6 and then discharged via a line 29, while the residual gas, after heating in passages 30 of the exchanger, is used to regenerate an adsorption bottle, the bottle 2B in the example under consideration, before being discharged via a pipe 31.
- a part of liquid oxygen 36 withdrawn at an intermediate level of the low pressure column is, after expansion in an expansion valve 32, stored in the reservoir 13 and pressurized by the pumped 14 and a liquid oxygen production is provided via a pipe 33 (medium purity) and / or 34 (high purity).
- Part of the medium purity liquid oxygen is vaporized after pressurization in the pump 14 in the heat exchanger 6.
- the pump 14 has a lower outlet pressure than the pump 12.
- the valve 32 is closed and no more medium pressure oxygen is withdrawn or the medium pressure oxygen flow is reduced.
- the withdrawal of the flow rate 16 is increased and more high purity oxygen and high pressure are pumped from the pump 12 into the exchanger 6.
- the outlet pressure of the compressor 1 is increased. as well as the flow rate of compressed air by adjusting the blades of the compressor 1. If there is no production of liquid oxygen, the sum of the flow rates 16 and 36 is constant, between the first and second steps because the flow of compressed air in the compressor 1 remains substantially constant between the two steps.
- the sum of the flow rates 16 and 36 is constant between the first and second steps, or a greater sum can be produced during the second step by reducing or even suppressing the production of liquid oxygen. If the production of liquid is reduced, a part of the air coming from the Claude 4 turbine will be sent to the atmosphere after being mixed with the waste gas 27.
- the installation represented in FIG. 2 is intended to produce oxygen. gaseous at two pressures and two purities.
- the double column is constituted, in a conventional manner, a medium pressure column 50 operating at about 6 bar and surmounted by a low pressure column 51 operating slightly above atmospheric pressure with, in the tank of the latter, a vaporizer-condenser 52 which puts in heat exchange relation the liquid oxygen of the tank of the low pressure column with the head nitrogen of the medium pressure column.
- the air compressor 44 of the installation directly compresses all the air at the first high pressure of the order of 23 bar, and a first stream of this air is treated as previously in the passages 53, the turbine 46 and the expansion valve 54 then sent to the base of the column 50.
- blower a single-wheel compressor whose energy expenditure, by the flow of gas treated and the compression ratio, is considerably lower than that of the main compressor 44 of the installation , and for example of the order of 2 to 3% of the latter.
- the compression ratio of such a blower is generally less than 2.
- Each of the blowers in question here comprises at its output a water or atmospheric refrigerant not shown.
- the liquid oxygen withdrawn from the bottom of the column 51 is fed by the pump 49 to the high pressure, then vaporized and reheated in passages 58 of the exchange line before being evacuated from the installation via a production line. 59 as a flow of high pressure, high purity oxygen gas.
- the liquid oxygen withdrawn at an intermediate level of the column 51 is fed by the pump 70 at medium pressure, then vaporized and reheated in passages 58 of the exchange line before being evacuated from the installation via a pipe as the flow rate of gaseous oxygen medium pressure and medium purity. Furthermore, in the installation of FIG.
- the second step either no more medium pressure oxygen is withdrawn or the medium pressure oxygen flow is reduced.
- the withdrawal of the flow of liquid oxygen in the vat of the low pressure column is increased and more high purity oxygen and high pressure are pumped from the pump 49 into the exchanger 6.
- the output pressure of the compressor 1 and the compressed air flow are increased by adjusting the blades of the compressor 1.
- the air flow is regulated by means of the blowers 70, 71.
- the sum of the flow rates 59 and 72 is constant, between the first and second steps.
- the compressed flow rate increases during the second step, the sum of the gaseous oxygen products may increase. Reducing or even suppressing the production of liquid oxygen also allows more variation in gaseous productions. If the liquid production is reduced, at least a portion of the air from at least one of the turbines 46, 72 will be sent to the atmosphere after being mixed with the waste gas 66 during the second step.
- a flow of air at atmospheric pressure is compressed to about 15 bar in a main compressor 1.
- the air is then optionally cooled, before being purified to remove impurities (not shown).
- the clean air is divided in two.
- Part of the air 3 is sent to a booster 5 where it is compressed to a pressure of between 17 and 20 bar and then the supercharged air is cooled by a water cooler 7 before being sent to the hot end of the main exchange line 9 of the air separation apparatus.
- the pressurized air 11 cools to an intermediate temperature before exiting the exchange line and being divided into two fractions. It is obviously possible for a fraction of the flow 11 to continue cooling down to the cold end of the exchange line 9 from which it will exit liquefied.
- a fraction 13 is sent into a turbine 17 and the remainder, a fraction 15 is sent into a turbine 19.
- the two turbines have the same temperature and suction pressure and the same temperature and outlet pressure but it is obviously possible that these temperatures and pressure are close to each other instead of being identical.
- the two turbine flows are mixed to form an air flow 21 of which a portion 121 is sent to the double column and the remainder 122 to the mixing column 300.
- the flow 122 constitutes a part of the flow 21 or possibly a fraction of the gas part of the flow 21 in the case where it would be two-phase. It is obviously possible to send all the flow 21 to the medium pressure column 100 and to leave a gaseous part 122 for sending to the mixing column, the medium pressure column replacing in this case the phase separator.
- the pressures of the medium pressure column and the mixing column may be different.
- the turbine 19 may be an insufflation turbine opening to the pressure of the low pressure column.
- Another part 2 of the air at 15 bars constituting the rest of the air is cooled in the exchange line at an intermediate temperature higher than the suction temperature of the turbines 17, 19, compressed in a second booster 23 until at about 30 bar and reintroduced into the exchange line 9 at a higher temperature to continue cooling.
- the air 37 to 30 bars approximately liquefies in the exchange line and the liquid oxygen 25 vaporizes in the exchange line, the vaporization temperature of the liquid being close to the suction temperature of the second blower 23.
- the liquefied air leaves the exchange line and is sent to the column system.
- the first booster 5 is coupled with one of the turbines 17, 19 and the second booster 23 is coupled with the other of the turbines 19, 17.
- the column system of an air separation apparatus is constituted by a medium pressure column 100 thermally connected with a low pressure column 200 to minaret, a mixing column 300 and an optional argon column (not shown).
- the low pressure column does not necessarily have a minaret.
- the medium pressure column operates at a pressure of 5.5 bar but can operate at a higher pressure.
- the air 121 coming from the two turbines 17, 19 is the flow rate delivered to the bottom of the medium pressure column 100.
- the liquefied air 37 is expanded in the valve 39 or possibly in a turbine and sent to the column system.
- Rich liquid 51, lower lean liquid 53 and upper lean liquid 55 are sent from the medium pressure column 100 to the low pressure column 200 after expansion stages in valves and subcooling.
- Liquid oxygen is pressurized by the pump 500 and sent as a pressurized liquid to the exchange line 9.
- Part of the liquid 501 can be stored as a liquid product.
- Other liquids, pressurized or not, can vaporize in the exchange line.
- Nitrogen gas is optionally withdrawn from the medium pressure column and is also cooled in the exchange line 9.
- Nitrogen 33 is withdrawn at the top of the low pressure column and heats up in the exchange line, after having served to sub-cool the reflux liquids.
- Residual nitrogen 27 is withdrawn from a lower level of the low pressure column and warms in the exchange line 9, after having been used to sub-cool the reflux liquids.
- the column can possibly produce argon by treating a flow
- the flow 52 is the tank liquid returned from the argon column, if there is one.
- the mixing column 300 is fed at the top with an oxygen rich liquid withdrawn at an intermediate level of the low pressure column 200. pressurized by the pump 600 and in the tank by a flow of gaseous air 122 from the turbines 17, 19.
- the mixing column operates essentially at medium pressure.
- a flow of oxygen gas 137 is withdrawn at the top of the mixing column and then warms in the exchange line 9 and a liquid flow 41 is withdrawn in the tank and sent to the low pressure column after expansion in a valve. It is possible to withdraw an intermediate flow from the column 300 which is sent to the low pressure column.
- the second step differs from the first in that the oxygen production of the mixing column is reduced or suppressed.
- the withdrawal of the flow of liquid oxygen in the tank from the low pressure column is increased and more high purity and high pressure oxygen from the pump 600 is vaporized in the exchanger 9 to form the flow 125.
- the outlet pressure of the compressor 1 and the compressed air flow rate are increased by adjusting the blades of the compressor 1.
- the air flow and its pressure are regulated by means of the booster 23.
- the air pressure 37 can be changed for the second step by changing the blades of the compressor 1 and / or those of the cold booster 23.
- the mixing column does not produce oxygen
- the surplus of the air is sent to the double column.
- the booster 23 compresses the air 2 to a higher pressure, which makes it possible to vaporize more liquid oxygen by increasing the tank withdrawal from the low pressure column to pressurize a larger flow rate in the pump 500.
- the only rich gas in oxygen product is oxygen medium pressure and medium purity.
- the second step is sent less air 122 in the tank of the mixing column. This receives less liquid oxygen and its operation is reduced. The surplus of the air is sent to the double column.
- the booster 23 compresses the air 2 to a higher pressure, which makes it possible to vaporize more liquid oxygen by increasing the tank extraction. of the low pressure column to pressurize a larger flow rate in the pump 500.
- the apparatus produces more medium pressure and medium purity oxygen than with the first step but continues to produce a reduced amount of low purity, low pressure oxygen.
- the sum of the flow rates 125 and 137 is constant, between the first and second steps.
- the compressed flow rate increases during the second step, the sum of the gaseous oxygen products may increase.
- the reduction or even the suppression of the liquid oxygen production 501 also allows more variation in the gaseous productions. If the liquid production is reduced, at least a portion of the air from at least one of the turbines 17, 19 will be sent to the atmosphere after being mixed with the waste gas 27 during the second step.
- the booster is driven by an air turbine but it will be easily understood that the booster could be driven by a nitrogen turbine, a steam turbine or other turbine present on the site.
- the invention makes it possible to solve the problem when two air separation devices produce high pressure oxygen. If one of the devices produces more or produces less, the other can increase the production of high pressure oxygen at the cost of producing oxygen medium pressure operating according to the invention.
- the additional air required can be supplied to the other apparatus from an air compressor or an air booster of the apparatus in stationary or reduced operation.
- the invention allows the other apparatus to provide up to 50% of the product previously from the device in stop or reduced walking. It is obviously possible to produce the two oxygen pressures during the first and possibly the second step by pumping a single flow of oxygen into a pump and by relaxing a portion. In this case, the flows will obviously have the same purity.
- the apparatus can also produce nitrogen and / or argon under pressure by spraying pumped nitrogen and argon (s). It is also possible to reduce or stop the production of nitrogen and / or argon under pressure during the second step compared to the production during the first step.
- the device can also produce liquid nitrogen as the final product during the first step. In this case, it is conceivable to reduce or stop the production of liquid during the second step.
- FIG 4 shows two air separation units ASU 1 and ASU 2, at least the first ASU 1 works according to the invention. Both devices are supplied with air by their respective compressors C1, C2. If the ASU 2 reduces its production of high purity oxygen 15, the ASU 1 begins to operate on the second step to produce more high pressure oxygen 15. To assist, purified or unpurified air can be sent from the compressor C2 to the ASU 1.
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Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
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BRPI0619924-0A BRPI0619924A2 (en) | 2005-12-15 | 2006-12-14 | cryogenic distillation air separation process |
KR1020087014219A KR101341278B1 (en) | 2005-12-15 | 2006-12-14 | Process for separating air by cryogenic distillation |
CN2006800473992A CN101331374B (en) | 2005-12-15 | 2006-12-14 | Process for separating air by cryogenic distillation |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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FR0553893A FR2895068B1 (en) | 2005-12-15 | 2005-12-15 | AIR SEPARATION METHOD BY CRYOGENIC DISTILLATION |
FR0553893 | 2005-12-15 |
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WO2007068858A2 true WO2007068858A2 (en) | 2007-06-21 |
WO2007068858A3 WO2007068858A3 (en) | 2007-09-13 |
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PCT/FR2006/051350 WO2007068858A2 (en) | 2005-12-15 | 2006-12-14 | Process for separating air by cryogenic distillation |
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KR (1) | KR101341278B1 (en) |
CN (1) | CN101331374B (en) |
BR (1) | BRPI0619924A2 (en) |
FR (1) | FR2895068B1 (en) |
RU (1) | RU2387934C2 (en) |
UA (1) | UA96431C2 (en) |
WO (1) | WO2007068858A2 (en) |
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WO2022053173A1 (en) * | 2020-09-08 | 2022-03-17 | Linde Gmbh | Method and plant for cryogenic fractionation of air |
EP4356052A1 (en) * | 2021-06-17 | 2024-04-24 | Linde GmbH | Method and plant for providing a pressurized oxygen-rich, gaseous air product |
CN115839600B (en) * | 2023-02-22 | 2023-05-05 | 中科富海(杭州)气体工程科技有限公司 | Cryogenic air separation plant |
Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB1216192A (en) * | 1967-01-23 | 1970-12-16 | British Oxygen Co Ltd | Air separation process |
JPS60125312A (en) * | 1983-12-12 | 1985-07-04 | Kawasaki Steel Corp | Method for controlling operation of equipment for generating oxygen and other gas in iron mill |
US5291737A (en) * | 1991-08-07 | 1994-03-08 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process or apparatus for distilling air and application in feeding gas to a steel mill |
US5596885A (en) * | 1994-06-20 | 1997-01-28 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for the production of gaseous oxygen under pressure |
US5941098A (en) * | 1996-12-12 | 1999-08-24 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and plant for supplying a variable flow rate of a gas from air |
FR2831249A1 (en) * | 2002-01-21 | 2003-04-25 | Air Liquide | Air separation in an apparatus containing at least two columns which can be operated normally or with air expanded to a low pressure in the turbine before distillation in the low pressure column |
FR2862128A1 (en) * | 2003-11-10 | 2005-05-13 | Air Liquide | PROCESS AND INSTALLATION FOR SUPPLYING HIGH-PURITY OXYGEN BY CRYOGENIC AIR DISTILLATION |
FR2865024A1 (en) * | 2004-01-12 | 2005-07-15 | Air Liquide | Separation of air by cryogenic distillation involves use of double or triple separation column and operating at high pressure |
US6945076B1 (en) * | 2002-09-11 | 2005-09-20 | L'air Liquide, Societe Anonyme Pour L'etude Et, L'exploitation Des Procedes Georges Claude | Production unit for large quantities of oxygen and/or nitrogen |
EP1586838A1 (en) * | 2004-04-06 | 2005-10-19 | Linde Aktiengesellschaft | Process and device for the production of variable amounts of a pressurized product by cryogenic separation of air |
-
2005
- 2005-12-15 FR FR0553893A patent/FR2895068B1/en not_active Expired - Fee Related
-
2006
- 2006-12-14 UA UAA200808102A patent/UA96431C2/en unknown
- 2006-12-14 KR KR1020087014219A patent/KR101341278B1/en active IP Right Grant
- 2006-12-14 WO PCT/FR2006/051350 patent/WO2007068858A2/en active Application Filing
- 2006-12-14 RU RU2008128818/06A patent/RU2387934C2/en active
- 2006-12-14 CN CN2006800473992A patent/CN101331374B/en active Active
- 2006-12-14 BR BRPI0619924-0A patent/BRPI0619924A2/en not_active Application Discontinuation
Patent Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB1216192A (en) * | 1967-01-23 | 1970-12-16 | British Oxygen Co Ltd | Air separation process |
JPS60125312A (en) * | 1983-12-12 | 1985-07-04 | Kawasaki Steel Corp | Method for controlling operation of equipment for generating oxygen and other gas in iron mill |
US5291737A (en) * | 1991-08-07 | 1994-03-08 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process or apparatus for distilling air and application in feeding gas to a steel mill |
US5596885A (en) * | 1994-06-20 | 1997-01-28 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for the production of gaseous oxygen under pressure |
US5941098A (en) * | 1996-12-12 | 1999-08-24 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and plant for supplying a variable flow rate of a gas from air |
FR2831249A1 (en) * | 2002-01-21 | 2003-04-25 | Air Liquide | Air separation in an apparatus containing at least two columns which can be operated normally or with air expanded to a low pressure in the turbine before distillation in the low pressure column |
US6945076B1 (en) * | 2002-09-11 | 2005-09-20 | L'air Liquide, Societe Anonyme Pour L'etude Et, L'exploitation Des Procedes Georges Claude | Production unit for large quantities of oxygen and/or nitrogen |
FR2862128A1 (en) * | 2003-11-10 | 2005-05-13 | Air Liquide | PROCESS AND INSTALLATION FOR SUPPLYING HIGH-PURITY OXYGEN BY CRYOGENIC AIR DISTILLATION |
FR2865024A1 (en) * | 2004-01-12 | 2005-07-15 | Air Liquide | Separation of air by cryogenic distillation involves use of double or triple separation column and operating at high pressure |
EP1586838A1 (en) * | 2004-04-06 | 2005-10-19 | Linde Aktiengesellschaft | Process and device for the production of variable amounts of a pressurized product by cryogenic separation of air |
Non-Patent Citations (1)
Title |
---|
PATENT ABSTRACTS OF JAPAN vol. 0092, no. 78, -& JP 60 125312 A (KAWASAKI STEEL CO; FUJI ELECTRIC CO LTD), 6 novembre 1985 (1985-11-06) -& JP 60 125312 A (KAWASAKI STEEL CO; FUJI ELECTRIC CO LTD) 4 juillet 1985 (1985-07-04) * |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2985305A1 (en) * | 2012-01-03 | 2013-07-05 | Air Liquide | Method for separation of air by cryogenic distillation for production of gas, involves pressurizing and vaporizing liquid flow in one of two exchange lines, and coupling cold booster with driving mechanism e.g. electrical motor |
Also Published As
Publication number | Publication date |
---|---|
FR2895068B1 (en) | 2014-01-31 |
RU2387934C2 (en) | 2010-04-27 |
FR2895068A1 (en) | 2007-06-22 |
UA96431C2 (en) | 2011-11-10 |
KR101341278B1 (en) | 2013-12-12 |
WO2007068858A3 (en) | 2007-09-13 |
CN101331374A (en) | 2008-12-24 |
CN101331374B (en) | 2012-05-30 |
BRPI0619924A2 (en) | 2011-10-25 |
KR20080074175A (en) | 2008-08-12 |
RU2008128818A (en) | 2010-01-20 |
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