CN106642993A - Air fractionation plant, operating method and control facility - Google Patents

Air fractionation plant, operating method and control facility Download PDF

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Publication number
CN106642993A
CN106642993A CN201610861067.3A CN201610861067A CN106642993A CN 106642993 A CN106642993 A CN 106642993A CN 201610861067 A CN201610861067 A CN 201610861067A CN 106642993 A CN106642993 A CN 106642993A
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CN
China
Prior art keywords
cooling
air
water
cooling device
temperature
Prior art date
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Pending
Application number
CN201610861067.3A
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Chinese (zh)
Inventor
S·多维
B·普尔尼格
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Linde GmbH
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Linde GmbH
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Publication date
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Publication of CN106642993A publication Critical patent/CN106642993A/en
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
    • F28C3/00—Other direct-contact heat-exchange apparatus
    • F28C3/06—Other direct-contact heat-exchange apparatus the heat-exchange media being a liquid and a gas or vapour
    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • 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
    • F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • 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
    • 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
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04775—Air purification and pre-cooling
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04793—Rectification, e.g. columns; Reboiler-condenser
    • F25J3/048—Argon recovery
    • F25J3/04806—High purity argon purification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
    • F28C1/00—Direct-contact trickle coolers, e.g. cooling towers
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • F25J2205/32—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as direct contact cooling tower to produce a cooled gas stream, e.g. direct contact after cooler [DCAC]
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
    • F25J2205/34—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes as evaporative cooling tower to produce chilled water, e.g. evaporative water chiller [EWC]
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/62—Purifying more than one feed stream in multiple adsorption vessels, e.g. for two feed streams at different pressures
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • F25J2205/70—Heating the adsorption vessel
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/84—Processes or apparatus using other separation and/or other processing means using filter
    • 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
    • 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
    • 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/12—Particular process parameters like pressure, temperature, ratios

Abstract

An air fractionation plant in which a cooling water circuit having a recooling apparatus is provided for cooling compressed air, where the recooling apparatus is configured for cooling cooling water using cooling air. The recooling apparatus is configured so as to cool the cooling water, at least at a wet bulb temperature of the cooling air of more than 289K, to a temperature which is not more than 3K above the wet bulb temperature. A corresponding operating method and a control facility are likewise provided.

Description

Air-separating plant, operational approach and control facility
The present invention relates to the air-separating plant, operation air-separating plant according to each preamble of independent claims Method and this air-separating plant control facility.
Prior art
For example H.-W.Haring (editor), Industrial Gases Processing, Wiley-VCH, 2006 year, It is especially in 2.2.5 parts, known in " Cryogenic Rectification " and describe by air-separating plant The cryogenic separation technology production liquid of air or gaseous air product.The present invention is applied to the various realities of respective air segregation apparatuss Apply scheme.
Air-separating plant has distillation column system, and for example, which is configurable to double tower system, especially classical woods moral (Linde) double tower system, but similarly it is configurable to three towers or many tower systems.Except being used to separating liquid or gaseous nitrogen Or the distillation column of oxygen (such as liquid oxygen LOX, gaseous oxygen GOX, liquid nitrogen LIN and/or gaseous nitrogen GAN), i.e., for the steaming of nitrogen oxygen separating Evaporate outside tower, it is also possible to provide for separating other constituent of air, the particularly distillation column of rare gas krypton, xenon or argon.
The distillation column system of air-separating plant is operated under the different operating pressure of its distillation column.For example, as it is known that it is double There is Tower System (height) to press tower and lower pressure column.The operating pressure of high-pressure tower be such as 4.3-6.9 bars, particularly from about 5.5 bars.Low pressure Tower is operated particularly under the operating pressure of about 1.4 bars in such as 1.2-1.7 bars.The pressure of indication refers to corresponding distillation herein The absolute pressure of tower bottom of towe.The pressure of following indication also can refer to " distillation pressure ", because sending out in distillation column at these pressures The fractional distillation of each feeding air that life is passed through.This is not precluded from the various location in distillation column system and can be mainly other pressures Power.
To be reached (such as main air compressor machine and rear air compressor machine) after the cooling of pressure using each air compressor machine or the combination of each air compressor machine Compressed air (feeding air) be passed through distillation column system.All air compressor machines can be multistage.Due to air-separating plant Middle about 95% energy consumption comes from above-mentioned air compressor machine, therefore has maximum energy-saving potential herein.The energy is needed fundamentally Cryogenic air separation process in hgher efficiency and device.
The content of the invention
In this context, the present invention provides the air-separating plant of the feature with each claim, operation air and separates The control facility of the method for device and this air-separating plant.
The feeding air of pressure is reached in air compressor machine in air-separating plant generally in different configuration of cooling facility In cooled down, so as to remove the heat produced in compression process.These chillers include for example being currently known in one Between individual or multiple compression stages and intercooler downstream and aftercooler.For example, especially can use from cooling water Compress in the main air compressor machine of the next effective cooling air segregation apparatuss of directly contact cooler operated by the cooling water in loop Air.It is furthermore possible to also provide the indirect heat exchanger for equally being operated using cooling water.In known method, feeding air Temperature subsequently become very low, i.e., in main heat exchanger, temperature be substantially less than 0 DEG C.
Cooled down especially for the energy consumption for reducing air compressor machine again.The temperature of cooling water is lower herein, can more cool down Plant air, so that the energy consumption of air compressor machine is reduced.In addition, the plant air thus can air inlet at a lower temperature Detached real process, including entering main heat exchanger.Therefore the heat changed in main heat exchanger is lower, so as to will exchange heat It is less that the volume of device is designed, and the cold produced by reducing pressure is also less.For example, the cold of generation is close to general 120- The low temperature of 200K can cause substantial amounts of energy loss, and this is substantially higher in being cooled down using cooling water in the case where ambient temperature is close to Energy loss.Furthermore, it is necessary to the larger cryogenic assembly (heat exchanger, turbine, valve) for doing is relatively costly.
The chilled(cooling) water return (CWR) of air-separating plant generally includes cooling device again, wherein the heating in the chilled(cooling) water return (CWR) Cooling water cooled down by transpiration-cooled mode using cooling air.Especially will be described below Know that the cooling tower of type can be used as cooling device again.For example, disclose in 0 644 390 A1 and JP 5885093A1 of EP Corresponding air-separating plant.Cooling air used herein is often generated from the surrounding of air-separating plant, therefore its With the temperature depending on surrounding, the pressure and the humidity depending on surrounding depending on surrounding.The wet bulb Temperature can be by above-mentioned three kinds of parameter determinations.
Wet bulb temperature is intended to indicate that measuring for cooling limit temperature (cooling limit temperature), i.e. cold But water is in the minimum temperature that accordingly can be reached by direct evaporating-cooling in theory in cooling device again.It is well known that in tide The moisture evaporation of wet structure is balanced each other with the water absorbing capacity of ambient atmosphere.Due to the cold produced by evaporation, cooling Limiting temperature is less than the air themperature as relative atmospheric humidity function.In evaporation cooling procedure, temperature drop is more, then week Enclose air drier.The wet bulb temperature and the temperature between the cooling water of the cooling for accordingly actually obtaining in cooling device again Difference referred to as cools down the limit temperature difference in the art.The performance of cooling device such as cooling tower is by specific surface area, the liquid of filler again What gas ratio and pressure drop were determined.In order to reach the little cooling limit temperature difference (cooling limit difference), it is essentially Desirable, because relatively low cooling water temperature has above-mentioned advantage, but thus result in for building again the very big of cooling device Capital cost.
Therefore, using the cooling limit temperature difference be consideration economically determining, which includes mentioned above each Aspect.Previously with regard in forced ventilation in the commercial plant again publication of cooling device, the cooling limit temperature difference is that 3 to 5K is usual Expression is economically viable, for example, with reference to " the Applied published by Z.K.Morvay ＆ D.D.Gvozdenac Industrial Energy and Environmental Management, Part III：Toolbox-Fundamentals For Analysis and Calculation of Energy and Environmental Performance, Toolbox 12：Cooling Towers ", Chichester, Wiley, 2008.But these data usually not indicate phase when being given The environmental condition answered and thus obtained wet bulb temperature.The cooling limit temperature difference of the cooling device with substantially less than 3K is in technology again On can be what is reached, but in general this is uneconomic.The corresponding relatively low cooling limit temperature difference is generally only used for experiment Room scale, the Thermodynamic Study of Wet Cooling for for example being published according to V.D.Papaefthimiou et al. Tower Performance, Int.J.Energ.Res.30 (6), 2006,411-426 that's how things stand.
Relevant cooling device again and its design further details refer to relevant speciality document, such as H.-D.Held, H.-G.Schnell, K ü hlwasser：Verfahren der Systeme der Aufbereitung und Kühlung Von S ü i β wasser, Brackwasser-und Meerwasser zur industriellen K ü hlung, the 5th edition, Vulkan, 2000, H.Rietschel, K.Fitzner, Raumklimatechnik, volume Two：Raumluft und Raumkuhltechnik, the 16th edition, Springer, 2008, J.J.McKetta, Encyclopedia of Chemical Processing and Design, volume 58, Marcel Dekker, 1997, P.N.Ananthanarayanan, Basic Refrigeration and Air Conditioning, the third edition, Tata McGraw-Hill, 2006, and B.Buecker, Power Plant Water Chemistry：A Practical Guide, PennWell, 1997 year.Especially It is to emphasize that the cooling limit temperature difference that can be realized by cooling device again can use known meter by those skilled in the art Calculation method is reliably predicted.Therefore, description below configures again cooling device so as to which is water-cooled to cooling higher than wet bulb The temperature of maximum temperature temperature value, for those skilled in the art, this considers that again the size of cooling device provides reference, so that its With above-mentioned characteristic, i.e., with the corresponding cooling limit temperature difference.Especially those skilled in the art will be it is considered herein that or with suitable Mode packing specific area, liquid-gas ratio and pressure drop are provided.
Advantages of the present invention
Unexpectedly, with regard to forced ventilation, the universal viewpoint of cooling device is contrary (for example, with reference to above-mentioned again The publication of Z.K.Morvay ＆ D.D.Gvozdenac), had recognized that according to the present invention, (totally gathered around based on total operating cost Have cost, TCO) consider, the cooling limit temperature difference provides economic interests for many air-separating plants when being less than 3K.Here, Under design condition and under given wet bulb temperature, according to capital value (representing per kilowatt hour by monetary unit, net present value (NPV), NPV) choosing Select the cooling limit temperature difference.Therefore, the device with identical capital value can not receive each environmental influence Under, obtain the cooling device again for removing identical specific heat.This allows to systematically select cooling tower according to capital value. According to viewpoint noted earlier of the invention, especially in the practical application in industry of such as air-separating plant, it is significantly higher than The cooling limit temperature difference of 3K is deemed appropriate.The publication of the Z.K.Morvay ＆ D.D.Gvozdenac for mentioning for several times above Thing propose it is a series of propose efficient measure, but do not reduce cooling down the limit temperature difference.
Therefore, the present invention proposes a kind of air-separating plant, provides the cooling with cooling device again in the apparatus Water loop, for cooling down compressed air, wherein cooling device cools down cooling water with using cooling air again described in configuration.This Bright air-separating plant is characterised by that cooling device is used at least in the cooling air higher than 289K again described in configuration Wet bulb temperature under, by it is described cooling be water-cooled to higher than the wet bulb temperature less than 3K temperature.In other words, by this Cooling device again in bright described air-separating plant, under specified requirementss, obtains the cooling limit temperature difference of 3K or less, especially Which is 2K or less, or 1K or less.
Find in the present invention, the discussion below for frequently referring in the literature is wrong：With the cooling pole less than 2K The cooling device again of the limit temperature difference is technically infeasible.Similarly, it is found that following common summary is incorrect：Only It is only when cooling down the limit temperature difference and being 3 to 5K economically viable.In the present invention it has been confirmed that with fixed and wet bulb temperature The feasibility and economic and practical index of the cooling device again of the unrelated cooling limit temperature difference is not predictive value.
Had been acknowledged according to the present invention and recorded below, the cooling limit temperature difference is reduced to below 3K, separates can air The economy of device is significantly improved at a temperature of the middle wet bulb temperature and high wet bulb higher than 289K.Therefore, the present invention is based on to having Close the important new assessment of the state of knowledge of the cooling Deethanizer design of regular air separating technology and low temperature process.
A kind of cooling device again that effectively can be operated is illustrated in the present invention, and cooling water can be cooled to very by which The minimum temperature (i.e. wet bulb temperature) being thermodynamically likely to be breached is close to, under the energy consumption of air-separating plant can be made notable Drop.This point can clearly be seen from Fig. 2 and 3 and be explained further below.Generally large-scale cooling device again effectively runs The extra capital cost (CAPEX) for producing is amortized in general one-year age by the operating cost (OPEX) saved 's.The large-scale amortization time of cooling device again is short (to be ordinarily be about as the totle drilling cost ratio of their duty air separations is less 2%).Table 1 summarises the capital cost and operating cost of conventional cooling device and cooling device again of the invention again, here It is corresponding cooling tower.
In economic evaluation, for example can be by the cooling device again of conventional design and cooling down again according to present invention design Equipment is contrasted, as shown in Figures 2 and 3.With (forced ventilation) cooling tower quilt for accommodating the tank of backwater as again Cooling device.Relatively low cooling limit temperature results in the need for larger cooling device again, and the same tank for expanding, therefore provides This cost is also higher.The mass flow of water is identical in both cases.The conclusive fact is, for same amount of cooling Water, in the case where cooling tower is larger, larger amount of air may flow through cooling device again, and these air can take away evaporation water, And while larger convection current cooling may be produced.The cooling water temperature in cooling tower of the invention is it reduced, and Due to the relatively low energy consumption of the air compressor machine and the cooling tower of energy source optimization, so that operating cost is relatively low.For this reason In the case of, it is assumed that power cost (power cost) in each case is.Report in table 1 per little When using 500,000 standard cubic meter plant air air-separating plant cooling device again result, and the fortune of 1 year Row cost.
Table 1：The capital cost and operating cost of conventional chilling tower and the cooling tower configured according to the present invention
For the purpose of the present invention, advantageously using the cooling device again for being configured in the following manner so which will be cold But it is water-cooled to higher than the wet bulb temperature at least temperature of 0.5K, for example also can be higher than at least 1K, the temperature of at least 1.5K or at least 2K Degree.Optimum scope between the minima and maximum of the cooling limit temperature difference can be obtained from above-mentioned consideration.
Air-separating plant of the invention can have the cooling device again of any configuration in principle, but especially excellent Choosing includes cooling tower.Especially there is force ventilated cooling device again or cooling tower Jing to be commonly used in air-separating plant, And it is proved to relatively low maintenance requirement.As described above, cooling tower especially can relatively simply pass through multiplying arrangement To reduce cooling limit temperature.
As described above, the cooling water cooled down using cooling device again is particularly suitable in respective air segregation apparatuss The rear cooling in compressor downstream, so as to the chilled(cooling) water return (CWR) of air-separating plant of the invention is advantageously comprised positioned at pneumatics The heat exchanger in the downstream of machine or corresponding air compressor machine level.For the purpose of the present invention, " air compressor machine " is single-stage or multistage setting, and which is matched somebody with somebody Put for increasing pressure, especially centrifugal air compressor (radical compressor) or vane type air compressor machine.One more Individual heat exchanger may reside in the downstream of one or more levels compressor.
In the present invention, the chilling temperature regional extent of the cooling device again can especially between 5-25K, especially It is, between 8-12K, to ordinarily be about 10K.
The method that the present invention extends further to operation air-separating plant, in said device offer have to cool down again and set Standby chilled(cooling) water return (CWR), which is used to cool down compressed air, wherein the configuration cooling device again is for cold using cooling air But cooling water.The method of the present invention is characterised by that the cooling device again is operated in this approach, at least higher than 289K Cooling air wet bulb temperature under, will cooling be water-cooled to higher than the wet bulb temperature less than 3K temperature.It is of the invention same Sample extends to the control facility of air-separating plant, and which is configured to realize such operational approach.In both cases, Above-mentioned relevant feature and advantage are can refer to.
Show the present invention below in conjunction with the accompanying drawings, the accompanying drawing shows the preferred embodiments of the invention.
Description of the drawings
Fig. 1 shows the air-separating plant of embodiment of the invention in the form of schematic process flow diagram.
Fig. 2 describes cooling water temperature and corresponding wet bulb temperature, to show embodiment of the present invention.
The extra cooling of Fig. 3 A and Fig. 3 B show present invention cooling water in the cards and the corresponding energy saved.
Accompanying drawing is described in detail
Fig. 1 shows the air point of particularly preferred embodiment of the invention in the form of schematic process flow diagram From device, and using numbering 100 referring to its package unit.
Feed air stream a is passed through air-separating plant 100 via filter 101, is compressed using main air compressor machine 102 and straight Cool down in connecing contact cooling device 103, the directly contact cooler is especially provided with the cooling current b from vapotron 104.It is logical Cross the pump individually not indicated the current b is introduced in the directly contact cooler 103.For cooling water supply stream b, institute State vapotron 104 and be provided with current c, a part for the current can also be precooled without vapotron 104, be passed through straight Connect contact cooling device 103.Current d takes from the directly contact cooler 103.
Shown current b, c and d, and the directly contact cooler 103 and vapotron 104 be integrated in number In 10 chilled(cooling) water return (CWR)s for referring to, which may also include other any current, directly or indirectly pump, heat exchanger etc., and these all do not have It is displayed in figure.For example, with extremely easy form, main air compressor machine 102 shows which has at least two compressor stages 1 here With 2, by intercooler 3 carrying out intercooling between the two compressor stages.The main sky of typical air-separating plant Press 102 includes the intercooler of 5 to 9 compressor stages and respective numbers.Shown in the cooling water of current s forms can be passed through Intercooler 3, which is configured to indirect heat exchange.Current s can especially be the tributary of the current c, i.e., equally in cooling water The cooling water circulated in loop 10.Analogue is also applied for other (afterwards) coolers as described below.Other current can be Any position is passed through in the chilled(cooling) water return (CWR) 10, for example, in order to compensate evaporating loss, and this sentences current e and represents.Additionally, water Cross-join between stream, adjusting means, measurement sensor etc. can be arranged on the vantage point in the chilled(cooling) water return (CWR) 10.
The center element of the chilled(cooling) water return (CWR) 10 is again cooling device 11, and which is here it is shown that as wet cooler, for example its Can be configured to force ventilated cooling tower.However, as described above, any other embodiment is also possible.Configuration institute Stating again cooling device 11 is used for the operation of the embodiment above of the invention.With at the air-separating plant 100 The big air-flow f of wet bulb temperature be passed through cooling device 11 again.For example, described in configuration, cooling device 11 treats cold for cooling again The water of current g but, in the illustrated case its formed by current d and e, be cooled to the wet bulb less than air stream f The temperature levels of temperature 3K.It is especially true when the wet bulb temperature of air stream f is higher than 289K.
The further process of air stream a by after compression and cooling, now with h referring to, corresponds mainly to routine Air-separating plant, such as H.W.Haring (editor), Industrial Gases Processing, Wiley-VCH, 2006 Year, in the air-separating plant particularly introduced in 2.2.5 parts " Cryogenic Rectification ".
Absorber group 105 is passed through by air stream h after compression and cooling, it include can blocked operation getter container, And can be regenerated by regeneration air stream i.The regeneration air stream i can pass through electric drive or steam drive regeneration gas is heated Device 106 is heated.In order to supply the regeneration air stream i, air-flow k, the supply of the air-flow can be used to be carried out below more Detailed description.
In adsorber group 105 by dry compressed air stream with I representing.According to the air-separating plant 100 Configuration, compressed air stream I can be collapsed into necessary or unnecessary pressure after it can make, and (the latter occurs in hyperbar work In the case of skill) under supply.As shown in example, the tributary m of compressed air stream I is passed through in rear compressor 107.After described The aftercooler of compressor 107, is not individually represented herein, can be carried out using the water from chilled(cooling) water return (CWR) 10 with sample cold But.
Embodiment according to being described, the tributary m of compressed air stream I and is not passed through by the tributary n of rear compression Main heat exchanger 108, then leaves equipment under different temperatures level.The air-flow m can be reduced pressure by turbogenerator 109, With the high-pressure tower 111 that distillation column system 110 is passed through after air-flow n combinations.Other tributaries of compressed air stream I can be formed, Cool down, compress afterwards, reduce pressure and equally in an advantageous manner, such as known throttling air-flow (not illustrated here) is passed through distillation In the tower of Tower System 110.
High-pressure tower 111 and lower pressure column 112 form the double tower system of known type together.In the example for showing, the steaming Evaporating Tower System also includes argon rectifying column 113 and pure argon column 114, but these towers are not required what is provided.Other can also be provided Distillation column.
The operation of the distillation column system 110 is known, therefore is no longer explained.In the shown example, remove Beyond other, the distillation column 110 is also fed with gaseous nitrogen stream o, and which is air-flow p forms " dirty nitrogen ", thus in main heat exchanger 108 Air-flow k and/or air-flow q can be formed after middle heating, and can be passed through in regeneration hot-air heater 106 or vapotron 104, liquid Oxygen-rich stream r can be divested.Except air-flow q, such as, it is possible to use cold nitrogen-enriched stream.Other fluids are no longer explained in detail. Any air-flow can be heated in main heat exchanger 108, be compressed or added in the upstream or downstream of main heat exchanger 108 Pressure, and merge with other air-flows and be divided into tributary.
Fig. 2 show 1 year in each month average cooling water temperature and corresponding wet bulb temperature, for showing this Embodiment in bright.By the cooling water temperature (in units of K) as vertical coordinate, the wet bulb temperature (in units of K) is Abscissa plots figure.In figure, the wet bulb temperature is represented in the form of data point 201, is being configured to the routine of cooling tower Design cooling device again in cooling water temperature represented in the form of data point 202 in figure, embodiment party of the invention The cooling water temperature of the cooling device again of case design in the form of data point 203 is represented in figure.
It is 8K that the conventional design causes the cooling limit temperature difference when wet bulb temperature is 289K.Described according to the present invention Embodiment, the cooling limit temperature difference is down to 3K from 5K.Using more efficient cooling tower so as to reducing the cooling limit The temperature difference, this can produce two kinds of effects, and the first is to provide colder cooling water, be for second to make the cooling water temperature and described The temperature difference between wet bulb temperature is relatively small.This means the cooling tower with relatively small cooling limit temperature difference design relative Colder month has fundamentally relatively small loss in efficiency.Large cooling column has more inefficient in relatively cold month The reason for loss is that water/gas ratio can change because of air.In two kinds of cooling tower variants, the mass flow of water is identical, crucial Factor is, for same amount of cooling water, in large cooling column, substantial amounts of air by the cooling tower, take away by these air Evaporation water, and while cool down with larger convection current.These effects serve positive role, especially in lower air temperatures When, air can take away a small amount of water.
Fig. 3 A and 3B show, and the corresponding energy Save (Fig. 3 B).The temperature difference in units of K in figure 3 a, the energy consumption difference in Fig. 3 B using in units of kW as vertical coordinate, with January Part (J) is drawn to December (D) as abscissa.
As can be seen that obtaining the cooler cooling water of actually colder 5K from Fig. 3 A.It can be seen that corresponding from Fig. 3 B For 270-450kW/ monthly, year averagely can save 340kW/ monthly to the energy consumption of saving.Energy consumption of compressor can decline 340kW, Corresponding to the 1.5% of compressor total energy consumption.

Claims (8)

1. air-separating plant (100), provide the chilled(cooling) water return (CWR) (10) with cooling device (11) again in the apparatus, are used for Cooling compressed air, wherein cooling device (11) cools down cooling water for using cooling air again described in configuration, its feature exists In, the configuration cooling device (11) again so as at least under the wet bulb temperature of cooling air for being higher than 289K, by the cooling It is water-cooled to the temperature less than 3K higher than the wet bulb temperature.
2. air-separating plant (100) according to claim 1, wherein described in configuration again cooling device (11) so as to will be cold But it is water-cooled to higher than the wet bulb temperature at least temperature of 0.5K.
3. air-separating plant (100) according to claim 1 and 2, wherein the cooling device again (11) is including cooling Tower.
4. air-separating plant (100) according to claim 3, wherein the cooling device again (11) is logical with forcing Wind.
5. the air-separating plant (100) according to aforementioned any one of claim, wherein the chilled(cooling) water return (CWR) (10) bag Include heat exchanger (103), the heat exchanger (103) be arranged in compressor (102, downstream 107).
6. the air-separating plant (100) according to aforementioned any one of claim, is provided in the apparatus from 5K to 25K Cooling zone scope.
7. the method for operating air-separating plant (100), provides the cooling water with cooling device (11) again in said device Loop (10) is for cooling down compressed air, wherein cooling device (11) is cooled down for using cooling air again described in configuration Water, it is characterised in that configure and operate the cooling device (11) again so as at least in the wet bulb of the cooling air higher than 289K At a temperature of, the cooling is water-cooled to into the temperature higher than the wet bulb temperature less than 3K.
8. method according to claim 7, wherein select and/or filler described in setting again in cooling device (11) ratio Surface area and/or liquid-gas ratio and/or pressure drop, so as at least higher than 289K cooling air wet bulb temperature under, will be described cold But it is water-cooled to the temperature less than 3K higher than the wet bulb temperature.
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