EP1094286A1 - Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft - Google Patents
Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft Download PDFInfo
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- EP1094286A1 EP1094286A1 EP00119941A EP00119941A EP1094286A1 EP 1094286 A1 EP1094286 A1 EP 1094286A1 EP 00119941 A EP00119941 A EP 00119941A EP 00119941 A EP00119941 A EP 00119941A EP 1094286 A1 EP1094286 A1 EP 1094286A1
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- European Patent Office
- Prior art keywords
- pressure column
- section
- condenser
- evaporator
- low
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- 238000000926 separation method Methods 0.000 title claims abstract description 14
- 238000000034 method Methods 0.000 title claims description 17
- 239000007788 liquid Substances 0.000 claims abstract description 80
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 56
- 238000001704 evaporation Methods 0.000 claims abstract description 42
- 230000008020 evaporation Effects 0.000 claims abstract description 38
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000001301 oxygen Substances 0.000 claims abstract description 37
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 37
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 28
- 238000010438 heat treatment Methods 0.000 claims abstract description 8
- 239000011552 falling film Substances 0.000 claims description 31
- 239000007789 gas Substances 0.000 claims description 14
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 claims description 5
- 238000012856 packing Methods 0.000 claims description 5
- 239000000047 product Substances 0.000 description 14
- 230000000694 effects Effects 0.000 description 3
- 239000006200 vaporizer Substances 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 241000883306 Huso huso Species 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000010408 film Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000004172 nitrogen cycle Methods 0.000 description 1
- 229910052756 noble gas Inorganic materials 0.000 description 1
- 150000002835 noble gases Chemical class 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000010409 thin film Substances 0.000 description 1
- 230000032258 transport Effects 0.000 description 1
Images
Classifications
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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
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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
- F25J3/04078—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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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- 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.
- F25J3/04884—Arrangement of reboiler-condensers
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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
- F25J3/04896—Details of columns, e.g. internals, inlet/outlet devices
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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
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
- F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
- F25J5/005—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger in a reboiler-condenser, e.g. within a column
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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
- 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
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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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
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- 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
- F25J2250/10—Boiler-condenser with superposed stages
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/20—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 low-temperature separation of air with the Features of the preamble of claim 1.
- the rectification system of the invention can be a classic two column system be designed, but also as a three or multi-column system. It can be in addition to the columns for nitrogen-oxygen separation further devices for Obtaining other air components, in particular noble gases, for example argon production.
- a heat exchanger designed as a condenser-evaporator has evaporation and Liquefaction passages. There is a liquid in the evaporation passages evaporates. They are in heat exchange contact with the liquefaction passages, in which a gaseous fraction in indirect heat exchange with the evaporating Liquid condenses. For example, details about evaporation processes the monograph "Evaporation and its technical applications" by Billet (1981) refer to.
- a condenser vaporizer can consist of one or more Heat exchanger blocks are constructed.
- a condenser-evaporator system exhibits one or more condenser evaporators.
- Circulation evaporator used as a condenser evaporator.
- This type is a Heat exchanger block arranged in a bath of the liquid to be evaporated.
- the Evaporation passages are open at the top and bottom. Liquid from the bath is drained from entrained upwards by the evaporation gas (thermosiphon effect) and flows back into the liquid bath. This is a natural one Liquid circulation only through the evaporation process and without supply given mechanical energy.
- the invention is therefore based on the object of a method of the beginning Specified type and a corresponding device that is economical and are particularly economical to operate and in particular one have particularly low energy consumption.
- the in the falling film evaporator (first section of the Condenser-evaporator system) non-evaporated liquid (second oxygen-rich liquid) becomes like in the usual falling film evaporation Conveyor supplied, for example a pump; this transports the However, liquid does not return to the entrance of its evaporation passages Falling film evaporator, but on a second section of the condenser-evaporator system.
- the first section requires only a relatively small amount Part, for example 30 to 50%, preferably 38 to 42%, of the total Evaporation performance of the condenser-evaporator system to take over.
- the natural liquid portion at the outlet of the is correspondingly large Evaporation passages of the falling film evaporator.
- the Conveying device allows the liquid, which has not initially evaporated, to continue second section of the condenser-evaporator system flow. This is whole or partially designed as a circulation evaporator. That is where the problem of Therefore, the need for an artificial fluid circulation is not or only in to a lesser extent.
- the oxygen product is preferably from in the process according to the invention subtracted from the second section of the condenser-evaporator system, either as a gas or as a liquid.
- a gaseous pressurized oxygen product can be obtained, by adding oxygen-rich liquid in a liquid state to an increased pressure brought and then evaporated against air or nitrogen (so-called Internal compression).
- the first section of the condenser-evaporator system of the invention can be arranged within the low pressure column or in a separate container.
- the method according to the invention and the corresponding device can be used for any Type of nitrogen-oxygen separation can be used, especially independently from the product purities in the heads and swamps of the columns.
- the steam that is in the evaporation passages of the second section of the Condenser-evaporator system is preferably not produced drawn off exclusively or mainly as a gaseous oxygen product, but at least half introduced into the low pressure column and there as rising steam used. If the entire oxygen product is liquid won and / or internally compressed, the whole in the second section of the condenser-evaporator system generated gas into the low pressure column to be led back.
- a third oxygen-rich liquid remains in the second section of the condenser-evaporator system as a non-evaporated part of the second oxygen-rich Liquid. It preferably collects in the liquid bath of the or one Circulation evaporator. It is preferred in the method according to the invention at least partially in the low pressure column and / or to the evaporation passages of the first section of the condenser-evaporator system liquid returned.
- This return line can be conveniently shared with the above mentioned return of steam to the low pressure column can be carried out, by placing an appropriate line at the level of the bath is arranged. With this, the liquid level in the circulation evaporator is at the same time regulated without the need for additional adjusting or regulating devices.
- the second section is partially designed as a second falling film evaporator, can also the already existing conveyor between the first and second section additionally for the generation of a liquid circulation on the second falling film evaporator can be used.
- the condensing-evaporator system liquefaction passages are preferably connected to the two columns as in claim 4 is described. This means that pumps can be dispensed with at these points, and even if the pressure column and low pressure column are arranged side by side are. (In this case, it is beneficial if the first section of the condenser-evaporator system below the bottom of the low pressure column and the second section of the condenser-evaporator system above the top one Bottom of the pressure column are arranged.)
- the first section designed as a falling film evaporator is preferably so dimensioned that in it that amount of nitrogen-rich liquid Condensation of a nitrogen-rich gas fraction is generated from the pressure column, which is required as a return in the low pressure column (plus if necessary the as unpressurized liquid product withdrawn).
- This is one example Share 30 to 50%, preferably 38 to 42% of the total Heat transfer capacity of the condenser-evaporator system.
- the rest of the Heat transfer (50 to 70%, preferably 58 to 62%) is done in the second section the condenser-evaporator system carried out so that there generates at least the amount of liquid required as a return in the pressure column becomes.
- the heating surface due to the spatial distribution of the heating surface be cheaper, in the first section a larger proportion of nitrogen-rich Condense fraction as described above, in order to suit the heating surface from second section (usually at the head of the pressure column) to the first section (in the Usually shift in the sump of the low pressure column. In this case, part of the first nitrogen-rich liquid, which is formed in the first section, as a return is applied to the pressure column. If necessary, the use of a Liquid pump required.
- the nitrogen-rich gas fraction is generally the top nitrogen Pressure column formed.
- the first section of the condenser-evaporator system is preferred trained exclusively as falling film evaporators. With the help of the above It can be dimensioned particularly cheaply as a single, relatively compact block be realized, or in the form of several (for example four) particularly low Blocks that are arranged side by side. An order immediately in Bottom of the low pressure column is also favorable for a low installation height of the plant and their insulation (cold box).
- the second section of the condenser-evaporator system can by at least two sections connected in series on the evaporation side are formed, the first of which as a falling film evaporator and the second is designed as a circulation evaporator.
- the Liquid that realized the evaporation passages of the falling film evaporator Flows out section, for example, in the liquid bath of the or one section implemented as a recirculating evaporator.
- the falling film evaporator-circulation evaporator combination can, for example, with continuous Liquefaction passages, as described in EP 795349 A in detail is described.
- the liquid from the bath of the Circulation evaporator in the low pressure column or to exit the Evaporation passages of the first section of the condenser-evaporator system returned and to increase the amount of liquid in the falling film evaporator trained section of the second section can be used.
- the invention also relates to a device for the low-temperature separation of air According to claim 9. Particularly advantageous embodiments of the device are described in claims 10 to 13.
- gaseous feed air 1 which was previously compressed, cleaned and cooled to approximately dew point (not shown), is fed to the pressure column 2 immediately above the sump.
- the pressure column 2 is part of a rectification system, which also has a low pressure column 3 and a main condenser in the form of a condenser-evaporator system 101, 102, 103.
- the air is broken down into top nitrogen in the pressure column 2 and into an oxygen-enriched liquid.
- the latter is not drawn off from the sump as usual, but rather from theoretical or practical floors higher via line 5.
- the oxygen-enriched liquid 5 is fed into the low-pressure column via an unillustrated line at an intermediate point 3 throttled.
- the low pressure column 3 there are one or more in the upper area Nitrogen products withdrawn (not shown). Below the bottom Rectification section is oxygen in the purity required for the product won. It flows as the first oxygen-rich liquid from the bottom floor or packing section of the low pressure column 3 and is in one Collector 7 collected. The first oxygen-rich liquid continues to flow to the upper end of the first section 101 of the condenser-evaporator system and is introduced into its evaporation passages. The first section 101 is as Falling film evaporator trained. About 28 to 30% of the first evaporate there oxygen-rich liquid 7 in indirect heat exchange with a first part 8 the nitrogen-rich gas fraction 4 from the top of the pressure column 2. This condenses nitrogen-rich gas 8 to a first nitrogen-rich liquid 9.
- the vapor 11 that is in the first section 101 of the condenser-evaporator system generated flows back to the lowermost rectifying section of the low pressure column and participates in countercurrent mass transfer within this column.
- the liquid remaining portion 12 forms a second oxygen-rich liquid. This is about Line 13 withdrawn and by means of a pump 14 to the second section of the Condenser-evaporator performed by a combination of another Falling film evaporator 102 and a circulation evaporator 103 is formed as in EP 795349 A is described in detail.
- the second oxygen-rich liquid flows in the evaporation passages of the another falling film evaporator 102 down and evaporates there to about 40%.
- the steam 15 formed is completely fed into the low pressure column 3 via line 16 returned, since in the example no oxygen is released directly as a gaseous product is removed from the rectification system.
- the line 16 also serves for Keeping the liquid level in the liquid bath 18 constant by removing excess Liquid together with the vapor generated in the second section 102, 103 Low pressure column 3 is performed.
- the remaining liquid 17 from the section 102 flows into the liquid bath 18 of the circulation evaporator 103 and forms together with the liquid 19 knocked over in the circulation evaporator, a third oxygen-rich Liquid.
- This is obtained as an oxygen product by partially over Line 20 drawn off, internally compressed by means of a pump 21, to the known one Evaporated way under increased pressure and finally as a gaseous pressure product is brought out.
- the liquefied air stream 24 can an intermediate point are introduced into the pressure column 2.
- the liquefaction passages of the further falling film evaporator 102 and the Circulation evaporators 103 are designed continuously. You are from a second Part 22 of the nitrogen-rich gas fraction 4 from the pressure column 2 is applied. The Nitrogen first flows through the falling film evaporator 102 and then through the circulation evaporator 103 and condenses at least partially, preferably practically complete. The resulting second nitrogen-rich liquid 23 becomes completely abandoned as a return to the pressure column 2.
- FIG. 2 shows in detail the connection between line 16 and the outside space around the two condenser-evaporators 102, 103, which form the second section of the condenser-evaporator system.
- the dimensions of the line are essentially designed according to the amount of gas to be transported. It is arranged in such a way that liquid overflows from the liquid bath of the circulation evaporator 103 and can flow back as film 26 on the underside of the line 16 into the low-pressure column 3 or into the liquid sump below the first falling film evaporator 101. As a result, the liquid level of the liquid bath of the circulation evaporator 103 is kept at a constant level without special control measures.
- FIG. 3 differs from FIG. 1 by an additional line 301, via which part of the first nitrogen-rich liquid 9 can be fed as a return to the pressure column 2.
- a liquid pump 302 is necessary to overcome the static height between the first section 101 of the condenser-evaporator system and the upper region of the pressure column 2.
- more heating surface can be installed in the first section 101, which is designed here as a bottom evaporator of the low pressure column 3.
- less heating surface is required for the second section 102, 103, in the example at the head of the pressure column 2.
- This allows the spatial division of the condenser-evaporator system to be optimized. In many cases, the advantage of this optimization is greater than the expenditure for the additional line 301 and the liquid pump 302.
- the entire Heating surface of the section 102 can be integrated into the first section 101, so that the second section of the condenser-evaporator system consists of only one Circulation evaporator 103 exists.
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- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
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- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
Claims (13)
- Verfahren zur Tieftemperaturzerlegung von Luft, bei dem verdichtete und vorgereinigte Einsatzluft (1) in ein Rektifiziersystem zur Stickstoff-Sauerstoff-Trennung eingeleitet wird, daseine Drucksäule (2),eine Niederdrucksäule (3) undein Kondensator-Verdampfer-System (101, 102, 103) zur Beheizung der Niederdrucksäule (3)
aufweist, wobeidas Kondensator-Verdampfer-System einen ersten Abschnitt (101) aufweist, der als Fallfilmverdampfer ausgebildet ist,eine erste sauerstoffreiche Flüssigkeit (6) aus der Niederdrucksäule (3) in die Verdampfungspassagen des Fallfilmverdampfers (101) eingeleitet und dort teilweise verdampft wird, wobei ein sauerstoffreicher Dampf (11) und eine zweite sauerstoffreiche Flüssigkeit (12) gebildet werden, und wobeider sauerstoffreiche Dampf (11) mindestens zum Teil in die Niederdrucksäule (3) zurückgeleitet wird,
dadurch gekennzeichnet, daß das Kondensator-Verdampfer-System einen zweiten Abschnitt (102, 103) aufweist, der mindestens teilweise als Umlaufverdampfer (103) ausgebildet ist und daß die zweite sauerstoffreiche Flüssigkeit (12, 13) mindestens teilweise mittels einer Fördereinrichtung (14) zu den Verdampfungspassagen des zweiten Abschnitts (102, 103) des Kondensator-Verdampfer-Systems geleitet wird. - Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß der in den Verdampfungspassagen des zweiten Abschnitts des Kondensator-Verdampfer-Systems erzeugte Dampf mindestens zur Hälfte in die Niederdrucksäule (3) eingeleitet (16) wird.
- Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß eine dritte sauerstoffreiche Flüssigkeit (18), die aus dem im zweiten Abschnitt (102, 103) des Kondensator-Verdampfer-Systems nicht verdampften Teil der zweiten sauerstoffreichen Flüssigkeit (12, 13) gebildet wird, mindestens teilweise in die Niederdrucksäule (3) und/oder zu den Verdampfungspassagen des ersten Abschnitts (101) des Kondensator-Verdampfer-Systems zurückgeleitet (16) wird.
- Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, daßim oberen Bereich der Drucksäule (2) eine stickstoffreiche Gasfraktion (4) erzeugt wird,ein erster Teil (8) der stickstoffreichen Gasfraktion (4) in die Verflüssigungspassagen des ersten Abschnitts (101) des Kondensator-Verdampfer-Systems eingeleitet und dort mindestens teilweise kondensiert wird, wobei eine erste stickstoffreiche Flüssigkeit (9) gebildet wird,ein zweiter Teil (22) der stickstoffreichen Gasfraktion (4) in die Verflüssigungspassagen des zweiten Abschnitts (102, 103) des Kondensator-Verdampfer-Systems eingeleitet und dort mindestens teilweise kondensiert wird, wobei eine zweite stickstoffreiche Flüssigkeit (23) gebildet wird,die erste stickstoffreiche Flüssigkeit (9) mindestens teilweise entspannt (10) und als Rücklauf auf die Niederdrucksäule (3) aufgegeben wird unddie zweite stickstoffreiche Flüssigkeit (23) mindestens teilweise als Rücklauf auf die Drucksäule (2) aufgegeben wird.
- Verfahren nach Anspruch 4, dadurch gekennzeichnet, daß ein Teil der ersten stickstoffreichen Flüssigkeit (9) als Rücklauf auf die Drucksäule (2) aufgegeben (301, 302) wird.
- Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß Drucksäule (2) und Niederdrucksäule (3) nebeneinander angeordnet sind, wobei der erste Abschnitt (101) des Kondensator-Verdampfer-Systems unterhalb des untersten Bodens beziehungsweise des untersten Packungsabschnitts der Niederdrucksäule (3) und/oder der zweite Abschnitt des Kondensator-Verdampfer-Systems oberhalb des obersten Bodens beziehungsweise des obersten Packungsabschnitts der Drucksäule (2) angeordnet sind.
- Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß der erste Abschnitt (101) des Kondensator-Verdampfer-Systems ausschließlich als Fallfilmverdampfer ausgebildet ist.
- Verfahren nach einem der Ansprüche 1 bis 7, dadurch gekennzeichnet, daß der zweite Abschnitt des Kondensator-Verdampfer-Systems durch mindestens zwei verdampfungsseitig seriell verbundene Teilabschnitte gebildet wird, von denen mindestens einer als Fallfilmverdampfer (102) und mindestens einer als Umlaufverdampfer (103) ausgebildet ist.
- Vorrichtung zur Tieftemperaturzerlegung von Luft mit einem Rektifiziersystem zur Stickstoff-Sauerstoff-Trennung, daseine Drucksäule (2),eine Niederdrucksäule (3) undein Kondensator-Verdampfer-System (101, 102, 103) zur Beheizung der Niederdrucksäule (3)
aufweist,wobei das Kondensator-Verdampfer-System einen ersten Abschnitt (101) aufweist, der als Fallfilmverdampfer ausgebildet ist,
und miteiner Einsatzluftleitung (1) zur Einleitung verdichteter und vorgereinigter Einsatzluft (1) in die Drucksäule (2),Mitteln zur Zuführung einer ersten sauerstoffreichen Flüssigkeit (6) aus der Niederdrucksäule (3) in die Verdampfungspassagen des Fallfilmverdampfers (101) undMitteln zur Rückführung von sauerstoffreichem Dampf (11) aus den Verdampfungspassagen des Fallfilmverdampfers (101) in die Niederdrucksäule (3),
dadurch gekennzeichnet, daß das Kondensator-Verdampfer-System einen zweiten Abschnitt (102, 103) aufweist, der mindestens teilweise als Umlaufverdampfer (103) ausgebildet ist und die Vorrichtung Mittel zur Einleitung einer zweiten sauerstoffreichen Flüssigkeit (12, 13) aus den Verdampfungspassagen des Fallfilmverdampfers (101) zu den Verdampfungspassagen des zweiten Abschnitts (102, 103) des Kondensator-Verdampfer-Systems aufweist, die eine Fördereinrichtung (14) umfassen. - Vorrichtung nach Anspruch 9, dadurch gekennzeichnet, daß Drucksäule (2) und Niederdrucksäule (3) nebeneinander angeordnet sind, wobei der erste Abschnitt (101) des Kondensator-Verdampfer-Systems unterhalb des untersten Bodens beziehungsweise des untersten Packungsabschnitts der Niederdrucksäule (3) und/oder der zweite Abschnitt des Kondensator-Verdampfer-Systems oberhalb des obersten Bodens beziehungsweise des obersten Packungsabschnitts der Drucksäule (2) angeordnet sind.
- Vorrichtung nach Anspruch 9 oder 10, dadurch gekennzeichnet, daß der erste Abschnitt (101) des Kondensator-Verdampfer-Systems ausschließlich als Fallfilmverdampfer ausgebildet ist.
- Vorrichtung nach einem der Ansprüche 9 bis 11, dadurch gekennzeichnet, daß der zweite Abschnitt des Kondensator-Verdampfer-Systems durch mindestens zwei verdampfungsseitig seriell verbundene Teilabschnitte gebildet wird, deren erster als Fallfilmverdampfer (102) und deren zweiter als Umlaufverdampfer (103) ausgebildet ist.
- Vorrichtung nach einem der Ansprüche 9 bis 11, dadurch gekennzeichnet, daß der Austritt (9) der Verflüssigungspassagen des ersten Abschnitts (101) des Kondensator-Verdampfer-Systems über eine Flüssigkeitsleitung (301) und gegebenenfalls über eine Flüssigpumpe (302) mit der Drucksäule (2) verbunden ist.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP00119941A EP1094286B1 (de) | 1999-10-20 | 2000-09-13 | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
Applications Claiming Priority (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19950570A DE19950570A1 (de) | 1999-10-20 | 1999-10-20 | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
DE19950570 | 1999-10-20 | ||
EP00102564 | 2000-02-07 | ||
EP00102564 | 2000-02-07 | ||
EP00119941A EP1094286B1 (de) | 1999-10-20 | 2000-09-13 | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
Publications (2)
Publication Number | Publication Date |
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EP1094286A1 true EP1094286A1 (de) | 2001-04-25 |
EP1094286B1 EP1094286B1 (de) | 2005-06-15 |
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Application Number | Title | Priority Date | Filing Date |
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EP00119941A Revoked EP1094286B1 (de) | 1999-10-20 | 2000-09-13 | Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft |
Country Status (4)
Country | Link |
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EP (1) | EP1094286B1 (de) |
AT (1) | ATE298070T1 (de) |
DE (1) | DE50010552D1 (de) |
ES (1) | ES2243182T3 (de) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1243882A1 (de) * | 2001-03-21 | 2002-09-25 | Linde Aktiengesellschaft | Argongewinnung mit einem Drei-Säulen-System zur Luftzerlegung und einer Rohargonsäule |
EP3910274A1 (de) * | 2020-05-13 | 2021-11-17 | Linde GmbH | Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungs anlage |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4006001A (en) * | 1974-01-18 | 1977-02-01 | Linde Aktiengesellschaft | Production of intermediate purity oxygen by plural distillation |
EP0410832A1 (de) * | 1989-07-28 | 1991-01-30 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Verdampfer-Kondensator für eine Zweisäulenanlage zur Luftzerlegung |
EP0469780A1 (de) * | 1990-07-31 | 1992-02-05 | The BOC Group plc | Tiefsieden von verflüssigtem Gas |
EP0795349A1 (de) * | 1996-02-14 | 1997-09-17 | Linde Aktiengesellschaft | Vorrichtung und Verfahren zum Verdampfen einer Flüssigkeit |
US5761927A (en) * | 1997-04-29 | 1998-06-09 | Air Products And Chemicals, Inc. | Process to produce nitrogen using a double column and three reboiler/condensers |
US5775129A (en) * | 1997-03-13 | 1998-07-07 | The Boc Group, Inc. | Heat exchanger |
-
2000
- 2000-09-13 EP EP00119941A patent/EP1094286B1/de not_active Revoked
- 2000-09-13 AT AT00119941T patent/ATE298070T1/de active
- 2000-09-13 ES ES00119941T patent/ES2243182T3/es not_active Expired - Lifetime
- 2000-09-13 DE DE50010552T patent/DE50010552D1/de not_active Revoked
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4006001A (en) * | 1974-01-18 | 1977-02-01 | Linde Aktiengesellschaft | Production of intermediate purity oxygen by plural distillation |
EP0410832A1 (de) * | 1989-07-28 | 1991-01-30 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Verdampfer-Kondensator für eine Zweisäulenanlage zur Luftzerlegung |
EP0469780A1 (de) * | 1990-07-31 | 1992-02-05 | The BOC Group plc | Tiefsieden von verflüssigtem Gas |
EP0795349A1 (de) * | 1996-02-14 | 1997-09-17 | Linde Aktiengesellschaft | Vorrichtung und Verfahren zum Verdampfen einer Flüssigkeit |
US5775129A (en) * | 1997-03-13 | 1998-07-07 | The Boc Group, Inc. | Heat exchanger |
US5761927A (en) * | 1997-04-29 | 1998-06-09 | Air Products And Chemicals, Inc. | Process to produce nitrogen using a double column and three reboiler/condensers |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1243882A1 (de) * | 2001-03-21 | 2002-09-25 | Linde Aktiengesellschaft | Argongewinnung mit einem Drei-Säulen-System zur Luftzerlegung und einer Rohargonsäule |
EP1243881A1 (de) * | 2001-03-21 | 2002-09-25 | Linde Aktiengesellschaft | Drei-Säulen-System zur Tieftemperatur-Luftzerlegung |
US6530242B2 (en) | 2001-03-21 | 2003-03-11 | Linde Aktiengesellschaft | Obtaining argon using a three-column system for the fractionation of air and a crude argon column |
US6564581B2 (en) | 2001-03-21 | 2003-05-20 | Linde Aktiengesellschaft | Three-column system for the low-temperature fractionation of air |
EP3910274A1 (de) * | 2020-05-13 | 2021-11-17 | Linde GmbH | Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungs anlage |
Also Published As
Publication number | Publication date |
---|---|
ES2243182T3 (es) | 2005-12-01 |
EP1094286B1 (de) | 2005-06-15 |
DE50010552D1 (de) | 2005-07-21 |
ATE298070T1 (de) | 2005-07-15 |
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