EP4127583A1 - Verfahren und anlage zur tieftemperaturzerlegung von luft - Google Patents
Verfahren und anlage zur tieftemperaturzerlegung von luftInfo
- Publication number
- EP4127583A1 EP4127583A1 EP21712713.3A EP21712713A EP4127583A1 EP 4127583 A1 EP4127583 A1 EP 4127583A1 EP 21712713 A EP21712713 A EP 21712713A EP 4127583 A1 EP4127583 A1 EP 4127583A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- rectification column
- liquid
- fed
- product
- column
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 63
- 238000000926 separation method Methods 0.000 title claims abstract description 51
- 239000007788 liquid Substances 0.000 claims abstract description 133
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 68
- 238000001704 evaporation Methods 0.000 claims abstract description 59
- 230000008020 evaporation Effects 0.000 claims abstract description 58
- 239000007789 gas Substances 0.000 claims abstract description 39
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 34
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000001301 oxygen Substances 0.000 claims abstract description 25
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 25
- 230000006837 decompression Effects 0.000 abstract 1
- 238000001816 cooling Methods 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 8
- 238000000354 decomposition reaction Methods 0.000 description 5
- 239000012530 fluid Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 230000014759 maintenance of location Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- HEZMWWAKWCSUCB-PHDIDXHHSA-N (3R,4R)-3,4-dihydroxycyclohexa-1,5-diene-1-carboxylic acid Chemical compound O[C@@H]1C=CC(C(O)=O)=C[C@H]1O HEZMWWAKWCSUCB-PHDIDXHHSA-N 0.000 description 1
- 238000004887 air purification Methods 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910052743 krypton Inorganic materials 0.000 description 1
- DNNSSWSSYDEUBZ-UHFFFAOYSA-N krypton atom Chemical compound [Kr] DNNSSWSSYDEUBZ-UHFFFAOYSA-N 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 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
- 238000005086 pumping Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 229910052724 xenon Inorganic materials 0.000 description 1
- FHNFHKCVQCLJFQ-UHFFFAOYSA-N xenon atom Chemical compound [Xe] FHNFHKCVQCLJFQ-UHFFFAOYSA-N 0.000 description 1
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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/0423—Subcooling of liquid process streams
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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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
- F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
- F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another 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
- F25J3/04248—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
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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
- F25J3/04284—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
- F25J3/04321—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 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
- F25J3/04436—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system
- F25J3/04454—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
- F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
- F25J2200/94—Details relating to the withdrawal point
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
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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
- F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/02—Internal refrigeration with liquid vaporising loop
Definitions
- the invention relates to a method and a system for the low-temperature decomposition of air according to the respective preambles of the independent claims.
- Air separation plants have rectification column systems which can be designed as two-column systems, in particular as double-column systems, but also as three or multi-column systems.
- rectification columns for obtaining nitrogen and / or oxygen in liquid and / or gaseous state, i.e. rectification columns for nitrogen-oxygen separation, rectification columns can be provided for obtaining further air components, in particular the noble gases krypton, xenon and / or argon.
- the rectification columns of the rectification column systems mentioned are operated at different pressure levels.
- Known double column systems have a so-called high pressure column (also referred to as a pressure column, medium pressure column or lower column) and a so-called low pressure column (upper column).
- the high pressure column is typically operated at a pressure level of 4 to 7 bar, in particular about 5.3 bar.
- the low-pressure column is operated at a pressure level of typically 1 to 2 bar, in particular about 1.4 bar. In certain cases, higher pressure levels can also be used in both rectification columns.
- the pressures specified here and below are absolute pressures at the top of the respective columns specified.
- air separation plants or corresponding processes are required which, in addition to relatively large amounts of nitrogen with a comparatively high purity (approx. 80 ppb oxygen content and less), also deliver certain amounts of an impure oxygen product.
- Corresponding nitrogen can be required, for example, in the manufacture of semiconductors or displays, whereas the impure oxygen is required for the glass production for corresponding displays on site.
- the air separation plants and processes known to date cannot provide impure oxygen as an additional product with the desired efficiency.
- a “condenser evaporator” is a heat exchanger in which a first, condensing fluid flow occurs in indirect heat exchange with a second, evaporating fluid flow.
- Each condenser-evaporator has a liquefaction space and an evaporation space.
- the liquefaction and evaporation space have liquefaction and evaporation passages.
- the condensation (liquefaction) of the first fluid flow is carried out in the liquefaction space, and the evaporation of the second fluid flow is carried out in the vaporization space.
- the evaporation and liquefaction spaces are formed by groups of passages which are in a heat exchange relationship with one another.
- the so-called main condenser which connects a high-pressure column and a low-pressure column of an air separation plant in a heat-exchanging manner, is designed as a condenser evaporator.
- the main condenser can in particular be designed as a single or multi-storey bath evaporator, in particular as a cascade evaporator (as described, for example, in EP 1 287 302 B1), or else as a falling film evaporator.
- the main condenser can be formed by a single heat exchanger block or by several heat exchanger blocks which are arranged in a common pressure vessel.
- a liquid flow is forced through the evaporation space by means of its own pressure and is partially evaporated there.
- This pressure is generated, for example, by a column of liquid in the feed line to the evaporation chamber.
- the height of this column of liquid corresponds to the pressure loss in the evaporation space.
- the gas or gas-liquid mixture emerging from the evaporation chamber can be passed on directly to the next process step or to a downstream device in a "once through" condenser evaporator of this type and is in particular not introduced into a liquid bath of the condenser evaporator from which the remaining liquid Portion would be sucked in again.
- expansion turbine or “expansion machine”, which can be coupled to further expansion turbines or energy converters such as oil brakes, generators or compressors via a common shaft, is set up to expand a gaseous or at least partially liquid stream.
- expansion turbines for use in the present invention can be designed as turbo expanders. If a compressor is driven with one or more expansion turbines, but without energy supplied externally, for example by means of an electric motor, the term “turbine-driven” compressor or, alternatively, “booster” is used. Arrangements of turbine-driven compressors and expansion turbines are also referred to as "booster turbines”.
- turbo compressors In air separation plants, multi-stage turbo compressors are used to compress the feed air to be separated, which are referred to here as "main air compressors".
- the mechanical structure of turbo compressors is fundamentally known to the person skilled in the art.
- the medium to be compressed is compressed by means of turbine blades which are arranged on a turbine wheel or impeller or directly on a shaft.
- a turbo compressor forms a structural unit, which, however, can have several compressor stages in a multi-stage turbo compressor.
- a compressor stage usually comprises a corresponding arrangement of turbine blades. All of these compressor stages can be driven by a common shaft. However, provision can also be made for the compressor stages to be driven in groups with different shafts, it also being possible for the shafts to be connected to one another via gears.
- the main air compressor is also distinguished by the fact that it compresses the entire amount of air fed into the rectification column system and used for the production of air products, that is to say the entire feed air.
- a “post-compressor” can also be provided, in which, however, only part of the amount of air compressed in the main air compressor is brought to an even higher pressure.
- This can also be designed as a turbo compressor.
- the use of a common compressor or compressor stages of such a compressor as the main air compressor and booster can also be provided.
- additional turbo compressors are typically provided in air separation plants in the form of the boosters mentioned, which are usually in the Compared to the main air compressor or the booster, however, only compress to a relatively small extent.
- liquids and gases can be rich or poor in one or more components, with “rich” for a content of at least 50%, 75%, 90%, 95%, 99%, 99.5%, 99, 9% or 99.99% and “poor” can mean a content of no more than 50%, 25%, 10%, 5%, 1%, 0.1% or 0.01% on a mole, weight or volume basis .
- the term “predominantly” can match the definition of "rich”.
- Liquids and gases can also be enriched or depleted in one or more components, these terms referring to a content in a starting liquid or a starting gas from which the liquid or the gas was obtained.
- the liquid or gas is "enriched” if this or this is at least 1, 1 times, 1, 5 times, 2 times, 5 times, 10 times 100 times or 1,000 times the content, and " depleted "if this or this contains at most 0.9 times, 0.5 times, 0.1 times, 0.01 times or 0.001 times the content of a corresponding component, based on the starting liquid or the starting gas. If, for example, “oxygen” or “nitrogen” is used here, this should also be understood to mean a liquid or a gas that is rich in oxygen or nitrogen, but does not necessarily have to consist exclusively of these.
- pressure level and "temperature level” to characterize pressures and temperatures, which is intended to express that corresponding pressures and temperatures in a corresponding system do not have to be used in the form of exact pressure or temperature values to realize the inventive concept.
- pressures and temperatures typically move in certain ranges, for example ⁇ 1%, 5% or 10% around a mean value.
- Corresponding pressure levels and temperature levels can be in disjoint areas or in areas that overlap one another.
- pressure levels include, for example, unavoidable or expected pressure losses.
- the pressure levels specified here in bar are absolute pressures.
- EP 3 521 739 A1 discloses a method for obtaining nitrogen in which the low-pressure column of the double-column system used has a top condenser (also known as "double column, double condenser” or DCDC method). This process provides for the use of forced flow condenser evaporators and a residual gas turbine to generate the process cooling capacity.
- the pressure in the evaporation chamber or the pressure gradient at the residual gas turbine is also low.
- the low evaporation pressure also results in low operating pressures in both rectification columns and a relatively low (approx. 8 to 8.5 bar) nitrogen product pressure.
- the necessary cooling capacity in the process is high (e.g. in the case of liquid production)
- the pressure in the evaporation chamber or the pressure gradient at the residual gas turbine is also high.
- the high evaporation pressure then leads to high operating pressures in both rectification columns and to a high nitrogen product pressure.
- the present invention is fundamentally based on the knowledge that a method of the type just described can be expanded with an additional column, as a result of which the problems mentioned can be overcome.
- a higher pressure can be used in the evaporation chamber of the top condenser of the low-pressure column, so that a corresponding increase in the nitrogen product pressure (e.g. up to the desired 11 bar) is possible without, however, having to increase the liquid capacity of the plant.
- the nitrogen product pressure e.g. up to the desired 11 bar
- only part of the residual gas from the evaporation space of the top condenser of the low-pressure column is expanded to perform work. As a result, the cooling capacity remains relatively low.
- Another part of the residual gas "drives" the rectification process in the additional rectification column. In the bottom of this additional rectification column, impure oxygen is obtained, which is then also obtained as an internally compressed stream.
- internal compression reference is made to the technical literature mentioned at the beginning.
- the method proposed according to the invention is significantly more efficient than the known methods explained above.
- the present invention proposes a method for the low-temperature separation of air in which an air separation plant with a first rectification column and a second rectification column is used, the first rectification column at a pressure level of 9 to 13.5 bar, in particular about 11.3 bar , is operated and the second rectification column is operated at a pressure level of 5.5 to 8.5 bar, in particular about 7.3 bar.
- the values mentioned are, in particular, pressure values at the top of the respective rectification columns.
- the first rectification column and the second rectification column can in particular be combined in the manner of a known double column.
- the first rectification column is fed with cooled compressed air and the second rectification column is fed with liquid from the first rectification column or liquid formed therefrom.
- this does not exclude that further feed streams can also be fed into the first and second rectification column and represents only a minimum requirement for the implementation of the present invention.
- liquid from a rectification column or "liquid formed therefrom” is used in a certain way, the "liquid formed therefrom” is to be understood in particular as liquid, for the formation of which the liquid used directly from the corresponding rectification column is used is used, and that this is changed in its composition without complete evaporation, but possibly by evaporation of part of its components. Cooling, heating, pressurization and relaxation can also be provided.
- first condenser-evaporator which in particular represent the main condenser connecting the first and second rectification columns in a heat-exchanging manner and can be designed as a forced-flow condenser-evaporator
- overhead gas of the first rectification column is condensed and liquid from the second rectification column or liquid formed therefrom is condensed within the scope of the present invention (see above) to obtain a gas phase, which is referred to here as the first evaporation product for later reference only.
- the latter liquid is in particular a bottom liquid from the second rectification column or a liquid which is formed from a corresponding bottom liquid.
- a second condenser-evaporator which can also be designed as a forced-flow condenser-evaporator
- overhead gas of the second rectification column is condensed and further liquid from the second rectification column or liquid formed therefrom is evaporated to obtain a second evaporation product.
- This further liquid can also be, in particular, bottom liquid from the second rectification column or liquid which is formed from such bottom liquid.
- a first portion of the second evaporation product is expanded, heated and removed from the process by means of an expansion machine.
- This first component so-called impure nitrogen, can for example be released directly into the atmosphere or, if necessary, used beforehand to regenerate adsorber units for air purification.
- this proportion - and thus the achieved cooling capacity - is lower than in conventional processes.
- Overhead gas of the first rectification column is carried out in the context of the present invention as a pure nitrogen product from the process.
- this pure nitrogen product can be made available to a consumer at a corresponding pressure level.
- a third rectification column is used in the context of the present invention. This is operated at a pressure level of 1.1 to 2.5 bar, in particular about 1.4 bar, in particular at the top of the third rectification column.
- a rectification is driven in the third rectification column using further residual gas.
- This is achieved by means of a third condenser evaporator in which a second portion of the second evaporation product is condensed and bottom liquid of the third rectification column or liquid formed therefrom is evaporated to obtain a third evaporation product.
- the second portion of the second evaporation product condensed by means of the third condenser evaporator is then at least partially fed into the third rectification column.
- the third rectification column is fed with unevaporated further liquid from the second rectification column or liquid formed therefrom and further bottom liquid from the third rectification column or liquid formed therefrom is internally compressed and carried out as the aforementioned impure oxygen product from the process.
- the further bottom liquid of the third rectification column, and thus the impure oxygen product is formed in particular with an oxygen content of 85 to 99.8%, for example 90 to 99.8%, for example with an oxygen content of 96.8%. So it is not necessarily a product commonly referred to as impure oxygen with up to 98% oxygen.
- the pure nitrogen product can in particular have a residual content of 10 ppm oxygen or less, in particular 5 ppm oxygen or less, to be provided.
- the production amount (ie the amount of product exported in each case) for the impure oxygen product can be, for example, 5 to 10%, in particular approx. 8.7%, based on the pure nitrogen product. In an embodiment explained below, this amount can also be up to 25%.
- Liquid nitrogen can also be withdrawn, although an amount of liquid nitrogen product is typically less than 1%, in particular less than 0.5%, for example approx. 0.1%, of the amount of the pure nitrogen product.
- Other air products are typically not formed or not formed in a greater amount than the aforementioned air products.
- the second condenser evaporator is operated at an evaporation pressure level of 2 to 5 bar, in particular approx. 3.6 bar.
- this evaporation pressure level is coupled to a certain extent with the rectification pressure levels in the first and in the second rectification column.
- the first portion of the second evaporation product which is expanded, heated and removed from the method by means of an expansion machine, is fed to the expansion machine in the context of the present invention, in particular at the evaporation pressure level.
- bottom liquid from the second rectification column can be partially evaporated by means of the first condenser evaporator while retaining the first evaporation product and an unevaporated residue.
- a first part of the unevaporated remainder can be evaporated by means of the second condenser evaporator to obtain the second evaporation product.
- the composition can be changed by achieving a depletion of low boilers in the first condenser evaporator (or enrichment of high boilers). If, on the other hand, there is complete evaporation, as in the second condenser evaporator, there is no change in the composition, since a corresponding depletion or enrichment effect does not occur.
- a second part of the unevaporated residue can be fed into the third rectification column.
- the unevaporated further liquid from the second rectification column or the liquid formed therefrom, with which the third Rectification column is fed, and the second portion of the second evaporation product condensed by means of the third condenser-evaporator, or its portion which is fed into the third rectification column are both fed into the third rectification column in a head region, whereby a "head region" is understood to mean a region above which there are no further separating devices.
- liquid can be used as the non-evaporated further liquid from the second rectification column or the liquid formed therefrom with which the third rectification column is fed, which is via a side take-off from the second rectification column and thus with a lower oxygen content than the bottom liquid , is taken.
- the third rectification column can in particular have a first separation section and a second separation section arranged above the first separation section, the unevaporated further liquid from the second rectification column or the liquid formed therefrom, with which the third rectification column is fed, to the third rectification column above of the second separation section, and wherein the second portion of the second evaporation product condensed by means of the third condenser-evaporator or its portion which is fed into the third rectification column is fed to the third rectification column between the first separation section and the second separation section.
- the cooled compressed air with which the first rectification column is fed can, in one embodiment of the present invention, be exclusively gaseous, cooled or partially pre-liquefied compressed air that is no longer compressed to the pressure level at which the first rectification column is operated.
- the cooled compressed air with which the first rectification column is fed comprises gaseous, cooled compressed air that is no longer compressed to the pressure level at which the first rectification column is operated, and also liquefied air that is compressed to a pressure level which is above the pressure level at which the first rectification column is operated, and which is then liquefied and let down in the first rectification column.
- the aforementioned product quantities are also present in this embodiment Impure oxygen of up to 25%, for example approx. 20%, of the product quantities of pure nitrogen, can be produced.
- a separate air compressor can be used to further compress the air to be liquefied.
- the third rectification column can have 15 to 25, in particular 20, theoretical dividing trays.
- the first rectification column can have 50 to 70, in particular 60, and the second rectification column 40 to 60, in particular 50, theoretical separation trays.
- Figures 1 to 5 show an air separation plant according to embodiments of the invention in a simplified, schematic representation.
- FIG. 1 an air separation plant according to an embodiment of the invention is illustrated in the form of a schematic process flow diagram and denoted as a whole by 100.
- input or process air P is sucked in via a filter 1 by means of a main air compressor 2.
- a main air compressor 2 After pre-cooling in heat exchangers (not specifically designated) and a direct contact cooler operated with water W, the correspondingly compressed air is fed to an adsorber station 3, where undesired components such as water and carbon dioxide are removed.
- the air is then fed in the form of a feed air stream a to a main heat exchanger 4 of the air separation plant 100 and removed from it at the cold end.
- the feed air stream also denoted by a, is fed into a first rectification column (high pressure column) 11 of a distillation column system 10 which, in addition to the first rectification column 11, also has a second rectification column (low pressure column) 12 formed as a double column with the first rectification column 11 and a third rectification column 13.
- first rectification column 11 a top gas and a bottom liquid are formed, the bottom liquid from the first rectification column 11 being passed here completely in the form of a stream b through a subcooling countercurrent 5 and fed into the second rectification column 12.
- second rectification column 12 an overhead gas and a bottom liquid are formed.
- a part of the top gas of the first rectification column 11 is condensed by means of a first condenser-evaporator 111 (main condenser), which is designed here as a forced-flow condenser-evaporator. Another part of the top gas is drawn off in the form of a stream c, passed through the subcooling countercurrent 5 and the main heat exchanger 4 and released as pure nitrogen product C.
- the condensed portion of the top gas of the first rectification column 11 is returned to the first rectification column 11 in the form of a stream d.
- a portion of the bottom liquid of the second rectification column 12 is also evaporated by means of the first condenser evaporator 111. The vaporized portion rises in the second rectification column 12.
- a second condenser evaporator 121 is used to condense overhead gas from the second rectification column 11, which is fed to the second condenser evaporator 121 in the form of a stream e.
- the condensed overhead gas is partly returned to the second rectification column 12 and partly made available as liquid nitrogen product E. Further top gas of the second rectification column 12 can be withdrawn from this in the form of a stream f, passed through the subcooling countercurrent 5 and the main heat exchanger 4 and made available as a further nitrogen product F under pressure.
- Liquid collected in a liquid retention device at the top of the second rectification column 12 can be returned by means of a pump 6 in the form of a stream g through the subcooling countercurrent 5 and to the first rectification column 11 ("back pumping"). At this point, a partial flow of the material flow used to form the liquid nitrogen product E can also be fed in, which is expanded to subcool the liquid nitrogen product E.
- a first portion of the further bottom liquid evaporated by means of the second condenser evaporator 121 from the second rectification column 12 is expanded in the form of a stream i and before and after the expansion in the subcooling countercurrent 5 and heated in the main heat exchanger 4 and carried out from the process, ie released to atmosphere A and used as a regeneration gas in adsorber station 3 if necessary.
- a third condenser evaporator 131 which is designed as a bottom evaporator of the third rectification column 13
- a second portion of the by means of the second Condenser evaporator 121 evaporated further bottom liquid from the second rectification column 12 in the form of a stream k condensed.
- bottom liquid from the third rectification column 13 is also evaporated.
- the third rectification column 13 is also fed in the form of a stream I with non-evaporated further liquid from the second rectification column 12.
- Bottom liquid from the third rectification column 13 is internally compressed in the form of a stream m by means of a pump 8 and is carried out as an internally compressed oxygen product M from the process.
- the unevaporated further liquid from the second rectification column 12, with which the third rectification column is fed in the form of the stream I, is the bottom liquid of the second rectification column 12.
- the second portion of the means condensed by means of the third condenser evaporator 131 of the second condenser-evaporator 121 from the second rectification column 12 or its portion that is fed into the third rectification column 13 this is also fed into the third rectification column 13 in a head region.
- An additional feed of liquid nitrogen X is also illustrated.
- this feeding is carried out differently.
- liquid of a stream n is used, which is withdrawn from the second rectification column 12 via a side take-off.
- the third rectification column 13 has a first separation section 13a and a second separation section 13b arranged above the first separation section 13a, the unevaporated further one Liquid from the second rectification column 12, with which the third rectification column 13 is fed, ie the stream n, is fed to the third rectification column 13 above the second separating section 13b, and the second portion condensed by the third condenser evaporator 131 being the by the second condenser evaporator 121 evaporated further liquid from the second rectification column 12 or its portion that is fed into the third rectification column 13, i.e. the stream k, is fed to the third rectification column 13 between the first separation section 13a and the second separation section 13b.
- the cooled compressed air with which the first rectification column 11 is fed is exclusively gaseous, cooled or pre-liquefied compressed air, which in the main air compressor 2 is no longer the pressure level at which the first rectification column 11 is operated, was compressed.
- the cooled compressed air, with which the first rectification column 11 is fed here comprises the gaseous, cooled compressed air of the stream a, which was no longer compressed to the pressure level at which the first rectification column 11 is operated, but also liquefied air of a stream o, which was compressed by means of a booster 9 to a pressure level which is above the pressure level at which the first rectification column 11 is operated and which is then liquefied in the main heat exchanger 4 and expanded in the first rectification column 11.
- the passage for the liquid collected in a liquid retention device at the top of the second rectification column 12 at the top of the second rectification column 12, which is returned to the first rectification column 11, is typically omitted, even if both passages are still rudimentary shown in FIG.
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Abstract
Description
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EP20020131 | 2020-03-23 | ||
PCT/EP2021/025093 WO2021190784A1 (de) | 2020-03-23 | 2021-03-05 | Verfahren und anlage zur tieftemperaturzerlegung von luft |
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EP4127583A1 true EP4127583A1 (de) | 2023-02-08 |
EP4127583B1 EP4127583B1 (de) | 2024-05-01 |
EP4127583C0 EP4127583C0 (de) | 2024-05-01 |
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US (1) | US20230038170A1 (de) |
EP (1) | EP4127583B1 (de) |
KR (1) | KR20220156848A (de) |
CN (1) | CN115151771A (de) |
WO (1) | WO2021190784A1 (de) |
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US4715873A (en) * | 1986-04-24 | 1987-12-29 | Air Products And Chemicals, Inc. | Liquefied gases using an air recycle liquefier |
DE10027139A1 (de) | 2000-05-31 | 2001-12-06 | Linde Ag | Mehrstöckiger Badkondensator |
DE10153919A1 (de) * | 2001-11-02 | 2002-05-08 | Linde Ag | Verfahren und Vorrichtung zur Gewinnung hoch reinen Sauerstoffs aus weniger reinem Sauerstoff |
DE102009023900A1 (de) * | 2009-06-04 | 2010-12-09 | Linde Aktiengesellschaft | Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft |
EP2789958A1 (de) | 2013-04-10 | 2014-10-15 | Linde Aktiengesellschaft | Verfahren zur Tieftemperaturzerlegung von Luft und Luftzerlegungsanlage |
EP3290843A3 (de) * | 2016-07-12 | 2018-06-13 | Linde Aktiengesellschaft | Verfahren und vorrichtung zur erzeugung von druckstickstoff und flüssigstickstoff durch tieftemperaturzerlegung von luft |
DE102018000842A1 (de) | 2018-02-02 | 2019-08-08 | Linde Aktiengesellschaft | Verfahren und Vorrichtung zur Gewinnung von Druckstickstoff durch Tieftemperaturzerlegung von Luft |
EP3557166A1 (de) | 2018-04-19 | 2019-10-23 | Linde Aktiengesellschaft | Verfahren zur tieftemperaturzerlegung von luft und luftzerlegungsanlage |
WO2020187449A1 (de) * | 2019-03-15 | 2020-09-24 | Linde Gmbh | Verfahren und anlage zur tieftemperaturzerlegung von luft |
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- 2021-03-05 EP EP21712713.3A patent/EP4127583B1/de active Active
- 2021-03-05 CN CN202180016010.2A patent/CN115151771A/zh active Pending
- 2021-03-05 WO PCT/EP2021/025093 patent/WO2021190784A1/de unknown
- 2021-03-05 KR KR1020227033708A patent/KR20220156848A/ko active Search and Examination
- 2021-03-05 US US17/906,499 patent/US20230038170A1/en active Pending
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WO2021190784A1 (de) | 2021-09-30 |
US20230038170A1 (en) | 2023-02-09 |
EP4127583B1 (de) | 2024-05-01 |
CN115151771A (zh) | 2022-10-04 |
KR20220156848A (ko) | 2022-11-28 |
EP4127583C0 (de) | 2024-05-01 |
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