CN105143801A - Method and device for producing gaseous compressed oxygen having variable power consumption - Google Patents

Method and device for producing gaseous compressed oxygen having variable power consumption Download PDF

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Publication number
CN105143801A
CN105143801A CN201480018663.4A CN201480018663A CN105143801A CN 105143801 A CN105143801 A CN 105143801A CN 201480018663 A CN201480018663 A CN 201480018663A CN 105143801 A CN105143801 A CN 105143801A
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Prior art keywords
tributary
heat exchanger
oxygen
pressure
main heat
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CN201480018663.4A
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Chinese (zh)
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D·戈卢贝夫
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Linde GmbH
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Linde GmbH
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Application filed by Linde GmbH filed Critical Linde GmbH
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • F25J3/04418—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 with thermally overlapping high and low pressure columns
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04957—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipments upstream of the fractionation unit (s), i.e. at the "front-end"
    • 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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    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
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    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • 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
    • 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
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04472—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • 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
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2313/00—Compression machines, plants or systems with reversible cycle not otherwise provided for
    • F25B2313/031—Sensor arrangements
    • F25B2313/0314—Temperature sensors near the indoor heat exchanger
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2313/00—Compression machines, plants or systems with reversible cycle not otherwise provided for
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    • F25B2313/0315—Temperature sensors near the outdoor heat exchanger
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2700/00—Sensing or detecting of parameters; Sensors therefor
    • F25B2700/21—Temperatures
    • F25B2700/2115—Temperatures of a compressor or the drive means therefor
    • F25B2700/21151—Temperatures of a compressor or the drive means therefor at the suction side of the compressor
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    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2700/00—Sensing or detecting of parameters; Sensors therefor
    • F25B2700/21—Temperatures
    • F25B2700/2115—Temperatures of a compressor or the drive means therefor
    • F25B2700/21152—Temperatures of a compressor or the drive means therefor at the discharge side of the compressor
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
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    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/50—Oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/54—Oxygen production with multiple pressure O2
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    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention relates to a method and to a device for the variable production of compressed oxygen by means of low-temperature separation of air in a distillation column system which comprises a high-pressure column (5) and a low-pressure column (6). Process air in form of a total air stream (1) is cooled in a main heat exchanger (3). At least a part of the cooled process air is fed into the high-pressure column (5). A first oxygen stream (35) from the low-pressure column (6) is brought to an elevated pressure (36) in a liquid state, is vaporized, or pseudo-vaporized, and heated in the main heat exchanger (3), and is finally obtained as a gaseous compressed oxygen product. Prior to entering the main heat exchanger (3), a first and a second partial stream (12) of the process air are brought to a high pressure (9, 10), which is at least 4 bars higher than the operating pressure of the high-pressure column (5). The first partial stream is liquefied, or pseudo-liquefied, in the main heat exchanger (3), and is subsequently introduced into the distillation column system (14). The second partial stream (16) is expanded to perform work (17), and is subsequently introduced into the distillation column system (4). In a first operating mode, a first total air quantity is cooled in the main heat exchanger (3), and a first turbine amount as first partial stream (16) is fed to the expansion to perform work. In a second operating mode, a second oxygen stream (46) from an external source outside the distillation column system is introduced into the low-pressure column (6) in a liquid state. There is less total air (1) cooled in the main heat exchanger (3), and less air is fed to the expansion (17) to perform work than in the first operating mode.

Description

The method and apparatus of gaseous compressed oxygen is produced with variable energy consumption
Technical field
The present invention relates to the method producing gaseous compressed oxygen with variable energy consumption changeably according to claim 1.
Background technology
Such as by Hausen/Linden, Tieftemperaturtechnik [cryogenic technique], the second edition in 1985, chapter 4 (281st ~ 337 pages) discloses the method and apparatus for low temperature air separating.
Distillation column system can be configured to double tower system (such as traditional woods moral double tower system), or three towers or multitower system.Except the tower for nitrogen oxygen separating, this system can also comprise other devices for generation of high purity product and/or other constituent of air particularly rare gas, and such as argon is produced and/or krypton xenon is produced.
In this process, relatively evaporate with the oxygen product stream of liquid state compression and heat carrier, and finally obtain as gaseous compressed product.These methods are also referred to as interior compression.It is for generation of compressed oxygen.When supercritical pressure, there is not the phase transformation on practical significance, so product stream is " pseudo-evaporation ".
Be in the product stream that heat carrier under high pressure and (puppet) evaporate and relatively liquefy (or puppet liquefies, condition is under it is in supercritical pressure).Heat carrier is often formed by the air of a part, is " second tributary " of the feeding air of compression under existing situation; Sometimes this stream is also referred to as throttling stream, although it replaces choke valve also can expand in liquid turbine (DFE=" dense fluid expander ").
Such as by DE830805, DE901542 (=US2,712,738/US2,784,572), DE952908, DE1103363 (=US3,083,544), DE1112997 (=US3,214,925), DE1124529, DE1117616 (=US3,280,574), DE1226616 (=US3,216,206), DE1229561 (=US3,222,878), DE1199293, DE1187248 (=US3,371,496), DE1235347, DE1258882 (=US3,426,543), DE1263037 (=US3,401,531), DE1501722 (=US3,416,323), DE1501723 (=US3,500,651), DE253132 (=US4,279,631), DE2646690, EP93448B1 (=US4,555,256), EP384483B1 (=US5,036,672), EP505812B1 (=US5,263,328), EP716280B1 (=US5,644,934), EP842385B1 (=US5,953,937), EP758733B1 (=US5,845,517), EP895045B1 (=US6,038,885), DE19803437A1, EP949471B1 (=US6,185,960B1), EP955509A1 (=US6,196,022B1), EP1031804A1 (=US6,314,755), DE19909744A1, EP1067345A1 (=US6,336,345), EP1074805A1 (=US6,332,337), DE19954593A1, EP1134525A1 (=US6,477,860), DE10013073A1, EP1139046A1, EP1146301A1, EP1150082A1, EP1213552A1, DE10115258A1, EP1284404A1 (=US2003/051504A1), EP1308680A1 (=US6,612,129B2), DE10213212A1, DE10213211A1, EP1357342A1 or DE10238282A1, DE10302389A1, DE10334559A1, DE10334560A1, DE10332863A1, EP1544559A1, EP1585926A1, DE102005029274A1, EP1666824A1, EP1672301A1, DE102005028012A1, WO2007/033838A1, WO2007/104449A1, EP1845324A1, DE102006032731A1, EP1892490A1, DE102007014643A1, EP2015012A2, EP2015013A2, EP2026024A1, WO2009/095188A2 or DE102008016355A1 discloses interior compression method.
The oxygen demand of fluctuation often forces air separation equipment to be designed to produce with variable oxygen the variable operation carried out.On the contrary, by providing the different operational modes with different-energy consumption level, although constant or substantial constant ground production, still running air separation equipment changeably, can be significant.
Due to different factor the rechargeable energy of ever-increasing ratio (especially in generating), in industrial plant region, Electricity price fluctuation becomes increasing.By the impact of some seasonal move, Electricity price fluctuation amplitude is also determined by day-night cycle.
When electricity needs in electrical network is low (such as at night), there is power surplus.But this surplus should be avoided, therefore with lower price supply.If the electricity needs in electrical network increases (such as by day), then electricity price also increases.Depend on area and concrete framework conditions, the electricity price in somewhere can change 5 times or higher.
Therefore need to be equipped with the air separation equipment that can adapt to load fast and effectively.Because need the conveying keeping gaseous compressed oxygen constantly, so it is generally impossible that the short time closes this equipment.
Storage means is replaced with the energy supply (Springmann of compensated waving with regard to known use before more than 30 years, " Energieeinsparung " [energy-conservation], Linde-Symposium, " Luftzerlegungsanlagen " [air separation plant], Linde AG the 4th task meeting held 15-17 day in October, 1980, article H).But this needs cost higher in equipment and control technology.In addition, by US7,272,954 disclose and introduce in distillation column system when high electricity price by cryogenic liquid and utilize cold compressor to consume excessive cold; But also need the extra cost in equipment in the case.
The method of preamble according to claim 1 is disclosed by EP793070A2.
Summary of the invention
The object of the invention is to provide the method for aforementioned type and corresponding equipment, although allow this equipment run changeably in scope wide especially in its energy ezpenditure and work efficiently especially in the case, it needs the lower cost on equipment.
This object is realized by the feature of the characteristic of claim 1.
When low energy supply and high electricity price, this equipment runs in the second operational mode.In the case, by supply liquid oxygen, not only cold is introduced this equipment, and complete mask work.No longer need to produce in the device from the oxygen of outside supply.Correspondingly, the total air introduced in this equipment can reduce.The generation of cold also can reduce, and can reduce to zero in extreme circumstances.Therefore turbine stream (the second tributary) reduces or interrupts even completely.In the case, the amount of gaseous compressed oxygen product remains unchanged or substantially constant.At this, " substantially constant " should be understood to change and is less than 3%, is preferably less than 2%.
In the present invention, by second and three tributary of two booster compressors be connected in parallel (also referred to as " booster air compressor " (BAC)) for air; In other words, corresponding booster compressor designs for two-wire.This brings king-sized bandwidth, and wherein the total amount of feeding air and the energy ezpenditure of therefore this equipment are all variable.Relative to the first operational mode being configured to the design situation with high liquid production, by closing in two booster compressors, and another runs with underload (such as 0%), and the energy ezpenditure in the second operational mode reduces to 50%.First the main air compressor compressing total air stream can be multi-thread or optional one wire design in the case equally.These two booster compressors such as have 2 to 5 grades, particularly 3 to 4 grades.Certainly, in the present invention, the three or more booster compressor be connected in parallel can also be used, for second and the 3rd tributary of air; So booster compressor to be designed to three lines or more line structure.In upstream or the downstream of multi-thread booster compressor, can use other booster compressor, it separately or jointly compresses second and the 3rd tributary.
In category of the present invention, the first pressure (the first tributary, so-called throttling stream) and the second high pressure (the second tributary, so-called turbine stream) can be identical or different.Total air also can be compressed to the first or second high pressure; Alternatively, total air compressing to lower pressure, such as, adds line loss to high pressure pressure tower, and implements booster compression to the first and/or second tributary of air.Second tributary all or is substantially all introduced in high-pressure tower usually at least in part, preferably after its acting is expanded.
At this, " total air stream " should be understood to the amount of the air finally introduced in distillation column system.This occurs with the form in two, three or more tributaries in a different manner, and it flows through main heat exchanger at least one component.
The liquid oxygen (the second oxygen stream) supplied in the second operational mode (" the 3rd oxygen stream " of claim 3) can produce during the first operational mode in this equipment self; Then, " external source beyond distillation column system " is formed by liquid oxygen tank, will introduce in this liquid oxygen tank by the 3rd oxygen stream at least partially at standard run duration.Alternatively, the second oxygen stream can take from other source, such as liquid tank fully, partly or sometimes, and it is not by the distillation column system of this equipment, but by adjacent air separation equipment or loaded by tank car.
In the standard of this equipment is run, in distillation column system, except liquid oxygen, fluid product can also be produced, as liquid nitrogen and/or liquid argon.
Advantageously, in the present invention, meet at least one, preferred all conditions described in claim 2.Preferably, relative to the first operational mode (standard with liquid production is run), under the second operational mode (at the energy reduced for seasonable operation), the numerical value that stream reduces is in following number range:
Total air ... ... ... ... ... ..5 % by mole to 30 % by mole
Turbine amount (turbine stream) ... ... ... .10 % by mole to 100 % by mole
Usually fluid product is not produced in the second operational mode, if or argon production is set, then except argon, do not produce fluid product.
The energy supply effectively adapting to especially fluctuate can be realized by the method for claim 3, wherein under the first operational mode (mode standard), discharge the 3rd oxygen stream as fluid product from lower pressure column.Under the second operational mode (power saving operation), obtain few oxygen as fluid product, preferably do not produce.(LOX product) second liquid oxygen amount preferably fewer than the first liquid oxygen amount 50 % by mole to 100 % by mole.
In the second operational mode, preferably cold compression is not implemented to the process flow of distillation column system.Especially, in the second operational mode, do not use rotary machine, it does not also use in the first operational mode.Therefore, the hardware spending for variable operation is low especially.
At this, " cold compression " should be understood to gas compression processes, wherein by gas being starkly lower than environment temperature, particularly lower than the temperature of 240K under send to compression.
Therefore can especially effectively implement according to method of the present invention.The all colds by the confession of supply liquid carrying can be utilized, to reduce turbine air amount.Must booster compression be implemented by correspondingly few air, or by by total air compressing in the method for high pressure, by total air compressing to significantly lower pressure.
Preferably in the second operational mode, the acting in the second tributary is expanded and is stopped completely, and namely the second turbine amount is zero.
These two booster compressors can the separative aftercooler of tool separately; Alternatively, its compression heat is discharged in common aftercooler.
In principle, total air stream can only be made up of the first tributary (turbine stream) and the second tributary (throttling stream).Total air stream also can comprise other air substreams, and comprise Part I (direct air), it turbine expansion does not occur, and sends in distillation column system with gaseous state substantially, particularly high-pressure tower.At this, " substantially gaseous state " refers to and is entirely gaseous state or comprises the stream being less than 1 to 2 % by mole of liquid.As recited in claim 7, preferably total air stream is divided into three strands of air streams just.
In addition, the present invention relates to equipment according to claim 8.Can be supplemented by the apparatus characteristic of the feature corresponding to dependent method claims according to equipment of the present invention.
Variable operation pattern according to the present invention not only can be applied to the equipment designed for this variable operation; In addition, the invention still further relates to the method according to the existing cryogenic air separation plant of the transformation of claim 9 to 11.
In the case, the hardware of existing distillation column system must be changed hardly.If lack the circuit for liquid oxygen being supplied to lower pressure column, then naturally need to transform it.In some cases, also existing circuit can be utilized; Then, supplementary parts and the optional pump existed only is needed.In addition, change control device, the i.e. software of operation control system.Especially, need not transform rotary machine.If existing equipment only has single line booster compressor, then the second booster compressor can be an exception.
The present invention and other details of the present invention are set forth in more detail below according to the embodiment schematically shown in the accompanying drawings.
Accompanying drawing explanation
Figure 1 shows that the first embodiment not comprising argon and produce, and
Figure 2 shows that the second embodiment that there is argon and produce.
Detailed description of the invention
Pre-cooled and the purification of air of not shown main air compressor, air in FIG.Total air 1 of purification enters in the first operational mode (standard operation/design conditions) under the pressure of 5.8 bar.In main heat exchanger 3, Part I 2 is cooled to about dew point at this pressure, and introduces in the high-pressure tower 5 of distillation column system via circuit 4, this distillation column system additionally has lower pressure column 6 and main condenser 7.There is at the top of these two towers the operating pressure of 5.0 to 5.5 bar or 1.3 to 1.4 bar respectively.Alternatively, the pressure in these two towers can be increased to higher level roughly pro rata.
In the booster compressor 9,10 to be connected in parallel for a pair with aftercooler 11, implement booster compression to 58 to the Part II 8 of total air 1 cling to, and be supplied to main heat exchanger 3 as " the first tributary " 13 and " the second tributary " 16.First tributary is delivered to the cold junction of main heat exchanger, and pseudo-in the case liquefaction.After expanding in choke valve 15, it is mainly imported in high-pressure tower 5 with liquid state.Discharge the second tributary from main heat exchanger 3 at intermediate temperatures via circuit 16, in expansion turbine 17, acting is expanded to about high-pressure tower pressure.Isolate little liquid part in separator (phase separator) 18 after, the Part I of the second tributary and feeding air is supplied to high-pressure tower via circuit 4 jointly.Turbine 17 is braked by generator G.
Liquid 19 at the bottom of the tower of the oxygen coalescence of high-pressure tower is crossing cooling in cold counterflow heat exchanger 20, and is supplied to the centre position of lower pressure column 6 via circuit 21.Via circuit 22 and 23 directly again discharging the air be supplied in high-pressure tower at least partially, and be supplied to lower pressure column 6 after crossing cold 20.Impure liquid nitrogen 24 same excessively cold (20), then via circuit 25 as reflux supply to the top of lower pressure column 6.
The Part I 27 of the gaseous overhead nitrogen 26 of high-pressure tower 5 liquefies completely or almost entirely in main condenser 7.The Part I 29 of the liquid nitrogen 28 obtained in the case as reflux supply to the top of high-pressure tower 5.Part II 30,32 obtains as fluid product (LIN) after flash gas separation in mistake cold 20 and in separator (phase separator) 33.The Part II 39 of the gaseous overhead nitrogen 26 of high-pressure tower 5 heats in main heat exchanger, and obtains as gaseous compressed nitrogen product (PGAN) via circuit 40.
At the bottom of the tower of lower pressure column, (more accurately: the evaporating space from main condenser 7) discharges liquid oxygen 34.Its Part I flow to pump 36 as " the first oxygen stream " 35, and is compressed to the pressure of 30 bar at this with liquid state.(precritical in this embodiment) oxygen stream 37 is guided to the cold junction of main heat exchanger.It evaporates and is heated to about environment temperature in main heat exchanger 3.Via circuit 38, the first oxygen stream finally obtains as gaseous compressed oxygen product (GOXIC).
The Part II 44/45 of liquid oxygen 34 optionally after crossing cold 20 through being discharged as " the 3rd oxygen stream " by circuit 45, and to obtain as fluid product.Particularly be introduced in liquid oxygen tank (not shown) (LOX is to tank).
Circuit 46 for supplying " the second oxygen stream " from liquid oxygen tank at the bottom of the tower of lower pressure column; But it does not work in the first operational mode.
From the tower top of lower pressure column 6 gaseous state not purity nitrogen 41 heat in main heat exchanger 3 crossing in cold counterflow heat exchanger 20 and further, and to blow out to air via circuit 42, or be used as regeneration gas in unshowned air cleaning facility.
In the first operational mode, air turbine 17 works, and does not flow through bypass line 43.Liquid oxygen is discharged from distillation column system via circuit 45 equally.Extraly, nitrogen can obtain as fluid product (LIN), and obtains (not shown) as pure gaseous nitrogen by lower pressure column.
In the second operational mode (battery saving mode), shut-down circuit 45; Preferably do not produce liquid nitrogen (LIN) yet.On the contrary, via circuit 46, liquid oxygen is supplied to lower pressure column from distillation column system outside.In the case, the output of gaseous compressed oxygen 38/GOXIC remains unchanged.Relative to the first operational mode, total air 1 decreases about 32 % by mole, and Part II 8/12 even decreases 65 % by mole; Preferably, one in these two booster compressors 9,10 does not work, and another is with the power work reduced.Turbine 17 is static, and bypass 43 is opened, and little stream flows through, the corresponding passage of its purge main heat exchanger.Total air pressure is only 5.3 bar, is only 53 bar in the air pressure in booster compressor 9,10 downstream.In the case, in the second operational mode, under the pressure identical with the first operational mode, carry the gaseous compressed oxygen product (GOXIC) of identical amount.These numerical value are applicable to following situation, obtain about 25 % by mole of total oxygen product in the first operational mode as fluid product, obtain about 75 % by mole, under about 30 bar as gaseous state (internal compression) compressed products.In addition, in the case, the liquid nitrogen of amount roughly the same with liquid oxygen is produced.At this, two kinds of effects are strengthened mutually, thus allow the energy ezpenditure in main air compressor (total air) and booster compressor (the first and second tributaries) to reduce especially significantly: on the one hand, by supplying liquid oxygen (therefore no longer needing to produce from the air capacity of supply) from outside, total air reduces; On the other hand, LOX and the LIN product do not produced reduce further air and refrigeration requirement.Unlike this, following in the second value embodiment of pure gas equipment, the change of a description amount, this only produces by supplying outside LOX in the second operational mode.
In category of the present invention, pure gas equipment (the second operational mode) can be manufactured by the equipment (the first operational mode) for generation of fluid product, save many energy when high electricity price in the case.The method keeps efficient at this, this is because compressor does not run in bypass, and (mainly needed for purge heat exchanger passages) amount and low enter temperature (this temperature in the second operational mode significantly lower than the first operational mode) because few, the loss during throttling of turbine stream is smaller.Indeed achieve the effective operational mode of not carrying out liquid production.Extra energy saves the total air (driving-energy correspondingly reduced in unshowned main air compressor) coming from minimizing.Because unwanted cold exports, save the driving-energy in booster compressor 9/10 extraly.
In category of the present invention, also correspondingly can transform the existing liquid plant still not having circuit 46 according to Fig. 1.For this reason, only need this circuit 46 is installed, otherwise all parts remain unchanged.
The present invention can also correspondingly for not having in the method for booster compressor, wherein by total air compressing to apparently higher than high-pressure tower pressure (HAP high air pressure).Independently to this, turbine 17 replaces generator can be braked by the booster compressor for turbine air.The present invention also can be applied to have and so-calledly be blown into formula turbine (air from main air compressor does not import pressure column upon inflation, but import lower pressure column) or there is the method for more than one turbine, and be applied to the method with nitrogen cycle.
The difference of Fig. 2 and Fig. 1 is only that the argon increased is produced, and it only schematically shows (argon case) at this.It is connected with lower pressure column with high-pressure tower in the usual manner.
In the first numerical example, the equipment according to Fig. 2 can run as in figure 1.In the case, in the second operational mode, the amount and the total air that produce liquid argon LAR reduce pro rata.
Unlike this, () because do not obtain liquid oxygen product (and preferably yet not obtaining liquid nitrogen product LIN) in the first operational mode yet for second value embodiment.In the case, in the second operational mode, the product volume of gaseous compressed oxygen 38/GOXIC is also equal with the first operational mode.Relative to the first operational mode, total air decreases 10 % by mole, and Part II 8/12 decreases 25 % by mole.This also can be produced by single booster compressor (replacing two booster compressors be connected in parallel shown in the figure).
Difference to that indicated in the drawings, turbine stream 16 also can be discharged, namely under the pressure that the pressure of the throttling stream 13 of discharging than the outlet from booster compressor 9,10 is lower at the middle drain position of these two booster compressors 9,10.In principle, turbine 17 also can use booster compressor graduated application, and one or two in its further convection current 13 and 16 implements booster compression.

Claims (11)

1. produced the method for gaseous compressed oxygen with variable energy ezpenditure by low temperature air separating in distillation column system, this distillation column system has high-pressure tower (5) and lower pressure column (6), wherein
-feeding air is cooled in main heat exchanger (3) with the form of total air stream (1),
-feeding air of cooling is at least partially imported in high-pressure tower (5),
-(36) will be compressed from the first oxygen stream (35) of lower pressure column (6) with liquid state,
-the first oxygen stream (37) of compression evaporation or puppet in main heat exchanger (3) are evaporated and heating,
-the first oxygen stream (38) heated is obtained as gaseous compressed oxygen product,
-compression (9,10) before it enters in main heat exchanger (3) of first tributary (13) of feeding air is extremely exceeded the first high pressure of at least 4 bar than the operating pressure of high-pressure tower (5),
-make the first tributary in the first liquefied at high pressure or pseudo-liquefaction in main heat exchanger (3), subsequently in importing (14) this distillation column system,
-(9,10) are compressed to the second high pressure exceeding at least 4 bar than the operating pressure of high-pressure tower (5) in second tributary (16) of feeding air,
-the second tributary is only cooled to medium temperature in main heat exchanger (3),
-the second tributary (16) acting being cooled to medium temperature is expanded (17), import in (4) this distillation column system subsequently,
-wherein, in the first operational mode
-by the cooling in main heat exchanger (3) of the first total air,
-the first turbine amount is sent to acting as the first tributary (16) to expand,
-and wherein, in the second operational mode
-will the second total air cooling in main heat exchanger (3) of the first total air be less than,
-the second turbine amount being less than the first turbine amount is sent to acting as the second tributary expands (17),
It is characterized in that:
-in the second operational mode, the second oxygen stream (46) from the external source beyond this distillation column system is imported in lower pressure column (6) with liquid state, and
-in the first operational mode, by the first and second tributaries (13,16) in the booster compressor (9,10) to be connected in parallel for a pair jointly (8,12) implement booster compression.
2. method according to claim 1, is characterized in that, meets the following conditions one of at least:
-the second total air is less than the first total air at least 5 % by mole,
-the second turbine amount is less at least 10 % by mole than the first turbine amount, especially little at least 30 % by mole.
3., according to the method for claim 1 or 2, it is characterized in that:
-in the first operational mode, the 3rd oxygen stream is discharged from lower pressure column as fluid product in the scope of the first liquid oxygen amount, and
-in the second operational mode, the 3rd oxygen stream is discharged as fluid product in the scope of the second liquid oxygen amount being less than the first liquid oxygen amount,
-wherein the second liquid oxygen amount is particularly less at least 50 % by mole than the first liquid oxygen amount, especially little 100 % by mole.
4. according to the method for one of claims 1 to 3, it is characterized in that, in the second operational mode, cold compression is not implemented to the process flow of distillation column system.
5. according to the method for one of Claims 1-4, it is characterized in that, the second turbine amount is zero.
6. according to the method for one of claim 1 to 5, it is characterized in that, two booster compressors (9,10) have common aftercooler (11) or have aftercooler separately.
7. according to the method for one of claim 1 to 6, it is characterized in that, total air stream is made up of Part I (2) and Part II (8), wherein Part II (2) is made up of the first tributary (13) and the second tributary (16), especially Part I (2) does not carry out turbine expansion and is supplied in this distillation column system, especially in high-pressure tower (5) with gaseous state substantially.
8. produced the equipment of gaseous compressed oxygen with variable energy ezpenditure by low temperature air separating, it comprises
-there is the distillation column system of high-pressure tower (5) and lower pressure column (6),
-main heat exchanger (3) for feeding air is cooled with the form of total air stream (1),
-for the feeding air of cooling at least partially being imported the device in high-pressure tower (5),
-device (36) for compressing with liquid state from the first oxygen stream (35) of lower pressure column (6),
-for making the device of the first oxygen stream (37) of compression evaporation or pseudo-evaporation and heating in main heat exchanger (3),
-for obtaining the device of the first oxygen stream (38) of heating as gaseous compressed oxygen product,
-for first tributary (13) of feeding air being compressed to before it enters in main heat exchanger (3) device (9,10) of the first high pressure exceeding at least 4 bar than the operating pressure of high-pressure tower (5),
-for making the first tributary at the first liquefied at high pressure or the pseudo-device liquefied in main heat exchanger (3),
-device (14) in this distillation column system is imported for first tributary of (puppet) being liquefied,
-for second tributary (16) of feeding air being compressed to the device (9,10) of the second high pressure exceeding at least 4 bar than the operating pressure of high-pressure tower (5),
-device for the second tributary in main heat exchanger (3) is discharged at intermediate temperatures,
-for making the device (17) of the second tributary (16) the acting expansion being cooled to medium temperature,
-for the first tributary of acting expansion being imported the device (4) in this distillation column system,
It is characterized in that,
-for the second oxygen stream (46) from the external source beyond this distillation column system to be imported the device in lower pressure column (6) with liquid state, and
-regulate the control device of following technological parameter:
-in the first operational mode
First total air of-cooling in main heat exchanger (3),
-the first turbine amount of doing work and expanding is sent to as the first tributary (16),
-in the second operational mode
Second total air of-cooling in main heat exchanger (3), it is less than the first total air,
-sending to acting as the first tributary expands the second turbine amount of (17), and it is less than the first turbine amount,
-with the amount of the second oxygen stream in liquid state importing lower pressure column (6), it is greater than the amount in the first operational mode.
9. for transforming low temp air fractionation system with the method run according to the method for one of claim 1 to 7, it is characterized in that, increasing the device being used for being entered by the second oxygen conductance in lower pressure column.
10. method according to claim 9, is characterized in that, extra booster compressor (10) and existing booster compressor (9) are connected in parallel.
11. methods according to claim 9 or 10, is characterized in that, except for except the device entered by the second oxygen conductance in lower pressure column and the extra booster compressor (10) optionally existed, do not change or substantially do not change described equipment.
CN201480018663.4A 2013-03-28 2014-03-27 Method and device for producing gaseous compressed oxygen having variable power consumption Pending CN105143801A (en)

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