CN105378411A - Method for producing at least one air product, air separation system, method and device for producing electrical energy - Google Patents

Method for producing at least one air product, air separation system, method and device for producing electrical energy Download PDF

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Publication number
CN105378411A
CN105378411A CN201480039508.0A CN201480039508A CN105378411A CN 105378411 A CN105378411 A CN 105378411A CN 201480039508 A CN201480039508 A CN 201480039508A CN 105378411 A CN105378411 A CN 105378411A
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China
Prior art keywords
air
pressure
stream
stress level
heat exchanger
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CN201480039508.0A
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Chinese (zh)
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CN105378411B (en
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A·阿列克谢耶夫
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Linde GmbH
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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
    • F25J3/04472—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
    • 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
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
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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
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    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
    • 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
    • F25J3/04006—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
    • F25J3/04084—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 nitrogen
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/02—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
    • F25J3/04254—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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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04—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
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    • F25J3/0426—The cryogenic component does not participate in the fractionation
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    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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    • 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
    • F25J3/04448—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 in a double column flowsheet with an intermediate pressure column
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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
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • F25J3/04575—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for a gas expansion plant, e.g. dilution of the combustion gas in a gas turbine
    • F25J3/04581—Hot gas expansion of indirect heated nitrogen
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
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    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the low pressure column
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
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    • 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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    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
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    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
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    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen
    • 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
    • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
    • F25J2260/50—Integration in an installation using oxygen, e.g. in the burner of a glass facility, waste incineration or oxygen based process [OBP] in general

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Abstract

The invention relates to a method for producing at least one air product, wherein an air separation system (100) is used which has a primary air compressor (10), a primary heat exchanger (20) and a distillation column system (30), and which comprises a first and a second operation mode, wherein, in the first operating mode, at least one liquid air product (LIN, LOX) produced in the distillation column system (30) is saved and, in the second operating mode, the at least one air product (LIN, LOX, LAIR) saved in the first operating mode and/or at least one additional liquid air product is supplied to the distillation column system (30). The method is characterized in that, in the second operating mode, at least one gaseous pressure flow (b - g) at a temperature level which lies below a hot-side temperature of the primary heat exchanger (20) is supplied to a cold compressor (45), compressed in the cold compressor (45) from a first above-atmospheric pressure level to a second above-atmospheric pressure level, and is supplied to at least one distillation column (31, 32) of the distillation column system (30) at the second above-atmospheric pressure level. The invention further relates to a corresponding air separation system (100) and to a method and to a device for producing electrical energy.

Description

The method and apparatus of the method for production at least one air products, air separation plant, generation electric energy
Technical field
The present invention relates to the method for the production at least one air products of the preamble according to independent claims, air separation equipment and produce the method and apparatus of electric energy.
Background technology
" condenser/evaporator " is the heat exchanger of instigating the first condensed fluid stream and the second evaporative fluid stream generation indirect heat exchange.Various condenser/evaporator all has the liquefied room and vaporization chamber that are made up of liquefier channel and evaporation channel respectively.First fluid stream condensation in liquefied room (liquefaction), second fluid stream evaporates in vaporization chamber.Vaporization chamber and liquefied room are formed by the passage group that there is heat exchange relationship each other.The vaporization chamber of condenser/evaporator can be configured to bath evaporimeter (Badverdampfer), falling film evaporator or force flow evaporator device.
In evaporimeter at the bottom of lower pressure column tower, at the bottom of the tower of lower pressure column, liquid evaporates at least partly in vaporization chamber.In lower pressure column central evaporator, the intermediate liquid of lower pressure column evaporates at least partly in vaporization chamber.
Prior art
The method of aforementioned type and the related device comprising three towers are known.
In the method for known generation electric energy, example is oxygen-enriched combusting method and so-called integrated gasification combined cycle plants (IntegratedGasificationCombinedCycle as is known, IGCC), need to use oxygen or oxygen coalescence admixture of gas, such as, for realizing burning or partial oxidation.Can adopt and such as be disclosed in Hausen/Linde, Tieftemperaturtechnik, 2.Auflage1985, Kapitel4 (Hausen/Linde, cryogenic technique, 1985 the 2nd edition, the 4th chapter, the 281 to 337 page) cryogenic air separation process and device oxygen or corresponding oxygen coalescence admixture of gas are provided.
In this type of method and apparatus (being called for short " air separation equipment " at this), use distillation column system, it such as can be configured to double tower system, particularly classical Linde double tower system, but also can be configured to three towers or multitower system.Device for extracting other constituent of air particularly rare gas such as krypton, xenon and/or argon can be set in addition.
The method and apparatus producing electric energy should for large loading range and fast load change design, thus can absorb because of other energy supplier can with or unavailable and power swing that is that cause.There is provided the air separation equipment of oxygen and/or corresponding admixture of gas also should realize the operational mode of flexibility and changeability in respective range for it.
Conventional air separation equipment also affects by electrical network utilization rate and electricity price that correspondingly intensity of variation is violent.
In the case, possible flexibility ratio depends on the liquefying power of air separation equipment.Available liquefying power is higher, then more low-price electricities can liquid air product form store.But the air separation equipment carrying out supplying for producing the method and apparatus of electric energy only has low liquefying power, this is because it is designed to produce in a large number the gaseous oxygen and gaseous nitrogen product that are extracted by this air separation equipment at ambient temperature.The chilling requirement of relevant device relatively low, therefore it also cannot provide enough colds to only provide relatively large liquid air product
Therefore, the liquefaction device (LIN liquefier, LOX liquefier or LAIR liquefier) of separation can be installed in relevant device, and access at liquefaction stage.By the refrigerating capacity of method or equipment (and therefore corresponding liquefying power) being designed to gaseous oxygen higher than actual aequum and gaseous nitrogen product, also certain flexibility can be realized.
If relatively large liquid air product is sent into corresponding air separation equipment, then may can enter this air separation equipment apparently higher than the cold of aequum.When not having counter-measure, this can cause each Temperature Distribution in heat exchanger to offset, and the temperature of one or more strands of stream of being discharged by heat exchanger becomes more and more lower.From specific limiting value, just cannot guarantee the reliability service of air separation equipment again.This problem can be resolved as air heat type, vapor heating type, gas-heated type, electric heating type heat exchanger or the heat exchanger that otherwise heats by using electro-heat equipment.But this type of solution is especially proved to be disadvantageous for the reason of energy aspect.
Summary of the invention
The object of the present invention is to provide the method for aforementioned type and corresponding device, its energy consumption excursion large and under all corresponding operational modes energy consumption lower.
This object is the method for the production at least one air products of feature by having independent claims, air separation equipment and the method and apparatus that produces electric energy realize.Preferred embodiment is each dependent claims and theme described below.
Being set forth in category of the present invention before attainable advantage, the some terms used in this application are illustrated.
" air separation equipment " is charging with the air of optional drying and purification, and it provides with the form of at least one compressed air stream by " main air compressor ".As previously mentioned, air separation equipment has for air separation being become its physical set to divide the distillation column system of particularly nitrogen and oxygen.As previously mentioned, for this reason by Air flow to close to its dew point, and to import in distillation column system.Unlike this, pure " air liquefaction plant " or " liquefying plant " do not comprise distillation column system.In addition, the structure of air liquefaction plant can correspond to the structure of the air separation equipment of supply air liquefaction product.Certainly, liquid air can also be produced as byproduct in air separation equipment.
" liquid air product " refer to any can at least by compressing air, cooling and expansion subsequently thus the product made with cryogenic liquid form.As previously mentioned, it especially can be liquid oxygen (LOX), liquid nitrogen (LIN), liquid argon (LAR) or liquid air (LAIR).At this, term " liquid oxygen " and " liquid nitrogen " also refer to that oxygen content and/or nitrogen content exceed the cryogenic liquid of atmospheric air respectively.Therefore it need not be and has the oxygen of high-load and/or the neat liquid of nitrogen.Therefore, liquid nitrogen not only refers to purity nitrogen or almost pure nitrogen, also refers to that nitrogen content exceedes the liquefied air admixture of gas of atmospheric air.Its nitrogen content is such as at least 90 % by mole, is preferably at least 99 % by mole.
" low temperature (deep cooling) " liquid or corresponding fluid, liquid air product, stream etc. refer to that its boiling point is far below respective environment temperature and be such as the liquid medium of 200K or lower, especially 220K or lower.In above-mentioned meaning, the example of cryogenic media is liquid air, liquid oxygen and liquid nitrogen.
" heat exchanger " for the indirect heat transfer between the stream that guides with adverse current each other at least two strands, the compressed air stream of such as one heat and one or more strands of cold flow or one low temperature liquid air products and one or more strands of hot-fluid.Heat exchanger can be formed by an independent heat transfer section or be formed by the heat transfer section of multiple parallel connection and/or series connection, such as, formed by one or more heat-exchangers of the plate type block.Heat exchanger, the feature such as used in air separation equipment is " main heat exchanger " of the major part cooling or heat stream to be cooled or to be heated with it, has " passage " of the fluid passage separated from one another being configured to comprise heat-transfer surface.Corresponding heat exchanger operationally has temperature different " hot side " and " cold side ".Temperature when " hot side " temperature of heat exchanger refers to that stream to be cooled is admitted to heat exchanger.Because multiply stream to be cooled may be had to be admitted to heat exchanger with different temperatures level, so the minimum or maximum temperature of stream to be cooled that hot side temperature also can relate to its mean value or be admitted to.
" compressor " is the device at least one gaseous flow being compressed at least one final pressure by least one initial pressure, and this gaseous flow sends into compressor under this initial pressure, and this gaseous flow is discharged by compressor assembly under this final pressure.Compressor forms a construction unit at this, but can have " compression stage " of the form of multiple known piston component, screw arbor assembly and/or impeller assembly and/or turbine assembly (i.e. axial-flow type or radial-flow type compression stage).This is also applicable to " main air compressor " of air separation equipment, it is characterized in that, is admitted to the whole or major part of the air capacity in air separation equipment with its compression.These compression stages especially utilize common drive unit such as to utilize common axle to drive.Main compressor and the rear compressor of multiple compressor such as air separation equipment can be connected to each other." rear compressor (supercharger) " is for improving the pressure of pressurized stream further.The feature of " cold compressor " is, at low temperatures, especially under cryogenic, will can flow feeding accordingly wherein.In the case, cold compressor is set up according to prior art.
" expansion turbine " can be connected to other expansion turbine or energy converter as oil brake, generator or compressor by common axle, expand for making gaseous flow or stream liquid at least partly.Expansion turbine especially can be used for the present invention as turbo-expander.If compressor is driven by one or more expansion turbine, but run when there is no the outside energy such as by motor supply, be then referred to herein as " turbine drives " compressor.The assembly (configuration) of turbine driven compressor and expansion turbine is also called " pressurized turbo machine "." pressurization nitrogen turbine (Druckstickstoffturbine) " or " PGAN turbine " refer to for making to produce in air separation equipment and the expansion turbine of the pressurized stream of the nitrogen enrichment of being discharged by distillation column system expansion in the application's category.Then the pressurized stream expanded such as can heat in main heat exchanger, and is disposed to surrounding environment.The expansion turbine being referred to as " middle-pressure turbine " is combined with the three-tower system comprising high-pressure tower, medium pressure column and lower pressure column specially.Middle-pressure turbine for make to be compressed by main air compressor and the compressed air stream optionally recompressed in rear compressor cool in main heat exchanger after expansion enter medium pressure column.Unlike this, " spray turbine (Einblaseturbine) " for make to be compressed by main air compressor and the compressed air stream optionally recompressed in rear compressor cool in main heat exchanger after expansion enter the lower pressure column of three towers or double tower system.Unlike this, be referred to as " restraining stream (Drosselstrom) " by the expansion valve stream entering high-pressure tower that expands.This stream in advance such as by be arranged among main air compressor or downstream rear compressor and/or be compressed to the stress level of the operating pressure higher than high-pressure tower by turbine driven compressor.
In the category of the application, " groove can system " refers to and comprises at least one configuration for the low-temperature storage tank of storing liquid air products.Corresponding groove can system has insulating part.
The application uses term " stress level " and " temperature levels " characterization pressure and temperature, shows thus, without the need to adopting corresponding pressure and temperature with the form of accurate force value or temperature value thus realizing design of the present invention.But these pressure and temperatures change usually in the particular range of the such as+/ – 1%, 5%, 10%, 20% or even 50% around mean value.Corresponding stress level and temperature levels can be in disjoint scope or in the scope that overlaps each other at this.Such as stress level especially comprises the inevitable or foreseeable pressure loss such as produced due to cooling effect.This is correspondingly also applicable to temperature levels.The stress level provided at these Israel and Palestine refers to absolute pressure.
Liquid air product or corresponding liquid flow can be transformed into gaseous state or supercriticality by heating.If heat under subcritical pressure boiler, then realize normal phase transformation by evaporation.If but at the heating under pressure liquid air product higher than critical pressure, then there is not the phase transformation on practical significance when being heated beyond critical-temperature, but become supercriticality by liquid state.If use term " evaporation " in the application's category, then it also comprises by the transformation of liquid state to supercriticality.
Advantage of the present invention
The present invention relates to a kind of method producing at least one air products, the method uses air separation equipment, and it has main air compressor, main heat exchanger and distillation column system.As previously mentioned, the method comprises first and second operational mode, wherein under this first operational mode, store at least one liquid air product resulted from this distillation column system, and under this second operational mode, the liquid air product store this at least one under this first operational mode and/or at least one affirm other liquid air products and/or the liquid air product carried by outside and/or otherwise temporary liquid air product (such as liquid air of not producing under this second operational mode, liquid nitrogen or liquid oxygen) send into this distillation column system.
According to the present invention, in the second operating mode, at least one gaseous state pressurized stream is admitted to cold compressor on the temperature levels of the hot side temperature lower than main heat exchanger, is compressed into the second superpressure stress level and on this second superpressure stress level, is admitted at least one destilling tower of distillation column system in this cold compressor from the first superpressure (superatmospheric pressure) stress level.This destilling tower runs with the operating pressure equaling the second superpressure stress level.Compared with prior art, the method has plurality of advantages:
As previously mentioned, generally can easily to cryogenic liquid or the liquid air product of the ice chest feeding small amount of air separation equipment, because because of insulation and (master) heat exchanger internal loss (the hot side temperature difference) cause, heat leak unavoidably, thus need certain cold all the time.This cold is provided by expansion turbine used usually.
If meet chilling requirement by above-mentioned feed energy, just this decompressor can be disconnected.When use so-called middle-pressure turbine and its inner expanding compressed air further, this can corresponding saving main air compressor and/or the driving power be located on this main air compressor rear compressor below.If realize correlation method on the injection turbine basis in order to make air expand to enter the lower pressure column of distillation column system used, then can obtain similar effect.If use the application graphic shown in pressurization nitrogen turbine or PGAN turbine, disconnect the turbine nitrogen that just can make to pressurize in a large number available, therefrom the energy that consumes of recyclable squeeze operation.Can use external expansion machine, corresponding pressurized stream is admitted to this decompressor after heating in front-mounted heating device for this reason, and it makes this pressurized stream be expanded to pressure needed for associated uses (being such as used as regeneration gas) again.
If will the cold input ice chest of needs be exceeded by feeding cryogenic liquid or liquid air product within one period of long period, just can cause the Temperature Distribution generation disadvantageous changes (" distortion ") in heat exchanger used, thus make the temperature of the stream of one or more outflow heat exchanger more and more lower.From a certain limit value, just cannot guarantee air separation equipment reliability service again or run by regulation.Further feeding cannot be realized again in the case, except non-used additional heating source improves the heat leak of ice chest.As previously mentioned, any one known heat-producing unit can be used for reaching this object, such as air heat type, vapor heating type, gas-heated type, electric power hot type heat exchanger or the heat exchanger otherwise heated.
With regard to above-mentioned situation, use cold compressor (as previously mentioned, namely intake air temperature is lower than the compressor of environment temperature) useful especially, because cold compressor is not only system heat supply, but affects by selective compression predetermined substance stream and improve overall procedure.Correlation method is illustrated by following Fig. 1 and Fig. 2.The method is that (under the corresponding cryogenic liquid of feeding or liquid air product " second " operational mode) disconnects corresponding expansion turbine (such as above-mentioned graphic shown pressurization nitrogen turbine with cold compressor compression, but also can be such as spray turbine) operational pressurization nitrogen quantity afterwards, then heats this pressurization nitrogen with preheater and makes it expand by independent expansion turbine.But the external expansion turbine with forward type preheater not under any circumstance all can obtain gratifying result of use, because this type of hardware component is very expensive and operation energy consumption is high.Such as, independent (middle pressure) vapour system must be set when running corresponding preheater usually.High loss can be produced thus.Therefore reducing costs with in energy-conservation meaning, do not using the method and apparatus of such device to be special Worth Expecting and favourable.
In air separation equipment, use cold compressor itself to be known.As disclosed in US7272954B2, cold compressor is used to compression restraining stream.But the target of this purposes and the method described by the application and relevant device is far from each other: as previously mentioned, compression restraining stream enters the operation of high-pressure tower to implement to expand just, thus reaches the object of extra refrigeration.Therefore, restraining stream is compressed into higher superpressure stress level, but on the superpressure stress level that this is higher, is not admitted to high-pressure tower, but reexpands before this.In addition within the scope of the present invention, the first superpressure stress level is lower than high-pressure tower operating pressure.
At respective air separation equipment by under " the first operational mode " repeatedly mentioned, not necessarily such as oxygen-rich combustion method or IGCC method provide gaseous air product.First operational mode also can comprise from relevant device extract liquid air products also (in electricity price cheap or electric energy superfluous period) imported ad hoc storage tank.The feature of the first operational mode is mainly, such as, in air separation equipment, produce extra cold by pressurization nitrogen turbine, injection turbine and/or middle-pressure turbine.At the most the air products being stored in groove can system on a small quantity is before this sent into distillation column system used and further separated process when needed, in order to avoid because of excessive input cold in the first operating mode and there is aforementioned ill effect.
And generally extra cold is not produced by pressurization nitrogen turbine, injection turbine and/or middle-pressure turbine under aforementioned " the second operational mode ", because the air products in this operating mode, being stored in storage tank is before this admitted to distillation column system used and further separates process when needed.Also can by attachment device or equipment, such as these air products be stored in storage tank by independent liquefier or provide.Second operational mode uses cold compressor to guarantee heat input, compresses corresponding pressurized stream simultaneously.
The present invention provides a kind of air separation equipment thus, even if it still can realize operation useful especially with low cost when being fed and being such as stored in the liquid air product of storage tank in a large number before this.Especially with comprise by the air separation equipment of hot type heat exchanger and comprise cold compressor compared with the equipment of external expansion turbine, can significantly reduce costs by this.
Certainly, the method also can comprise aforementioned first operational mode, in this operating mode, this at least one gaseous state pressurized stream and/or at least one other gaseous state pressurized stream in expansion turbine swell refrigeration ( entspannt).In the case, the method can switch on demand between two operational modes.
The method is preferably applicable to following situation: use distillation column system, it comprises high-pressure tower and lower pressure column, and wherein this high-pressure tower runs with the operating pressure higher than this lower pressure column.This type of distillation column system (system that such as double tower system or high and low pressure tower are separated) is substantially known to industry.Therefore the method is suitable for numerous existing air separation equipment and installs corresponding distillation column system additional.
In this type of distillation column system, the first stress level equals lower pressure column operating pressure, and/or the second stress level equals high-pressure tower operating pressure.The present invention realizes corresponding boost in pressure at this, and while quantitatively inputting cold, realize pressurized stream to import distillation column system.
If use distillation column system, it comprises medium pressure column further, and this medium pressure column runs with the operating pressure between the operating pressure of high-pressure tower and lower pressure column, just can realize special beneficial effect and processing procedure control more flexibly.
Correspondingly, now the first stress level can equal lower pressure column operating pressure, and the second stress level can equal the operating pressure of medium pressure column or high-pressure tower.As an alternative, the first stress level can equal medium pressure column operating pressure, and the second stress level can equal high-pressure tower operating pressure.
No matter which kind of situation, this at least one gaseous state pressurized stream all can extract by one destilling tower (the i.e. lower pressure column run for operating pressure with the first stress level from distillation column system, if there is medium pressure column, be then also optionally medium pressure column) the formation at least partially of stream.Through cold compressor compression after, can by this at least one gaseous state pressurized stream send at least partly the relatively high destilling tower of stress level (if extract from lower pressure column, then be medium pressure column or high-pressure tower, if extraction from medium pressure column, be then high-pressure tower).
As an alternative, this at least one gaseous state pressurized stream also can be provided by main air compressor by one and being formed at least partially of the stream cooled through main heat exchanger (namely such as part is admitted to the medium pressure column of distillation column system and is in " the middle baric flow " of relevant pressure).With after through cold compressor compression after, this gaseous state pressurized stream can be fed in the destilling tower that relevant pressure level is run.
Before being admitted to corresponding destilling tower, this at least one gaseous state pressurized stream also can converge with other streams at least one on the second stress level.If this second stress level such as equals high-pressure tower operating pressure, the gaseous state pressurized stream through corresponding compression just can be provided on this second stress level by main air compressor to one and the corresponding compressed air stream cooled through main heat exchanger converges.
If this compressed gaseous pressurized stream is not yet in nominal temperature, then this at least one gaseous state pressurized stream can after cold compressor compression at least partially in cooled in main heat exchanger.This is also a useful measure, deals with by selective thermal input the unfavorable situation causing main heat exchanger Temperature Distribution to change because of feeding liquid air product.
In the case can on demand contributing to arbitrarily heat exchanger feeding on the position obtaining good cooling effect and/or affect Temperature Distribution, for example, see Fig. 9 and Figure 10.Can by this at least one gaseous state pressurized stream after cold compressor compression in hot side or send into main heat exchanger cool on another temperature levels lower than the hot side temperature of main heat exchanger.
If this part through the gaseous state pressurized stream of cold compressor compression is heated and/or is exported air separation equipment at least partly in main heat exchanger, then the method also can obtain beneficial effect.Corresponding stream such as can be used as regeneration gas in the purifier comprising contactor, and is on pressure useful especially and temperature levels for this reason.
About the feature & benefits of air separation equipment of the present invention, refer to aforementioned advantages.This kind of air separation equipment has main air compressor, main heat exchanger and distillation column system and is suitable for running under aforementioned first operational mode and aforementioned second operational mode, be wherein provided with in order to store under this first operational mode at least one result from liquid air product in this distillation column system and under this second operational mode by this at least one liquid air product of storing under this first operational mode and/or other liquid air products at least one send into the device of this distillation column system.The bridgeware that related device such as can comprise manual switch part or adopt control technology and build.This air separation equipment has cold compressor.This be outside equipped with in order under this second operational mode by this at least one gaseous state pressurized stream on the temperature levels of the hot side temperature lower than main heat exchanger, send into this cold compressor, in this cold compressor by this at least one gaseous state pressurized stream be compressed to the second superpressure stress level from the first superpressure stress level, then by this at least one gaseous state pressurized stream on this second stress level, send at least partly the device of at least one destilling tower of this distillation column system.
About generation the inventive method of electric energy and the feature & benefits of apparatus of the present invention, also refer to foregoing teachings.The method and this device especially can be oxygen-rich combustion method or IGCC method and related device.
The present invention is elaborated referring to institute's accompanying drawings.
Accompanying drawing explanation
Figure 1 shows that the equipment schematic diagram when air separation equipment of non-invention is in the first operational mode;
Figure 2 shows that the equipment schematic diagram when air separation equipment shown in Fig. 1 is in the second operational mode;
The air separation equipment that Figure 3 shows that according to one embodiment of the present invention is in equipment schematic diagram during the second operational mode;
The air separation equipment that Figure 4 shows that according to one embodiment of the present invention is in equipment schematic diagram during the second operational mode;
The air separation equipment that Figure 5 shows that according to one embodiment of the present invention is in equipment schematic diagram during the second operational mode;
The air separation equipment that Figure 6 shows that according to one embodiment of the present invention is in equipment schematic diagram during the second operational mode;
The air separation equipment that Figure 7 shows that according to one embodiment of the present invention is in equipment schematic diagram during the second operational mode;
The air separation equipment that Figure 8 shows that according to one embodiment of the present invention is in equipment schematic diagram during the second operational mode;
When Figure 9 shows that the air separation equipment of foundation one embodiment of the present invention is in the second operational mode, the partial schematic diagram of the feasible program of cold compressor is set in this air separation equipment; And
When Figure 10 shows that the air separation equipment of foundation one embodiment of the present invention is in the second operational mode, the partial schematic diagram of the feasible program of cold compressor is set in this air separation equipment.
Detailed description of the invention
Peer component have in the drawings same-sign and will not repeat specification in the hope of short and sweet.
Fig. 1 is to Figure 10 shows that the equipment that part is identical and the icon of parts under different operational mode thereof, and the difference of these operational modes is mainly the position of multiple valve in respective lines, therefore liquid flow and gaseous flow are through distinct device parts.Valve does not give diagram.But blocking tube is made fork (-x-) online.
Fig. 1 is the equipment schematic diagram of the air separation equipment 110 of non-invention.Air separation equipment 110 is in the first operational mode in FIG, is admitted to this air separation equipment under this operational mode without the liquid air product in a large number from " external source " (such as storage tank or air liquefaction plant).Icon first operational mode such as produces liquid air product for or electric energy cheap in electricity price superfluous period, and wherein these liquid air product storages also prepare to be admitted to air separation equipment 110 under the second operational mode shown in Fig. 2 in corresponding storage tank.Other operational modes also can comprise only to be provided or mainly provides gaseous air product.
The core component of air separation equipment 110 comprises the main air compressor 10, main heat exchanger 20 and the distillation column system 30 that schematically show in figure, this distillation column system is configured to the multitower system comprising high-pressure tower 31, medium pressure column 32 and lower pressure column in illustrated embodiment, and wherein this lower pressure column has the first section 38 and the second section 33.This two section does not take the gas line k of any transformation measure to be connected by one, thus forms unified distillery, and this distillery is as good as with integral type lower pressure column in separating effect, pressure and temperature.
The top operating pressure of high-pressure tower 31 is such as 5.0 to 5.5 bar, and the top operating pressure of lower pressure column 33 is such as 1.3 to 1.4 bar.The operating pressure of medium pressure column 32 is between the operating pressure of high-pressure tower 31 and the operating pressure of lower pressure column 33.
In order to provide corresponding compressed air to distillation column system 30 or each tower, main air compressor 10 is configured to provide at least one first compressed air stream a and one second compressed air stream l.In the case, the stress level of the first compressed air stream a is that the operating pressure of high-pressure tower 31 is (therefore also known as " pressure-air ", HPAIR), the stress level of the second compressed air stream l is then the operating pressure of medium pressure column 32 (former also known as " middle pressure air ", MPAIR).
The presentation mode of corresponding compressed air stream a and l is known substantially, repeats no more herein.Such as, main air compressor 10 is by filter suction atmospheric air and by its multi-stage compression to above-mentioned pressure.Such as can extract the first compressed air stream a in multi-stage compression destination county, extract the second compressed air stream l in a middle position.This air can cool by carrying out indirect heat exchange with cooling water after compression in direct contact cooler.This cooling water can be provided by vaporization chamber cooler and/or external source.This compression cooling-air can be cleaned subsequently in purifier.This purifier can have the container that suitable sorbing material is housed for a pair.With rich nitrogen regeneration gas (referring to flow v, under associated description is shown in), purifier is regenerated herein.
In the illustrated embodiment, the first compressed air stream a passes the passage 21 of main heat exchanger 20 and is cooled to close to dew point in this place in aforementioned pressure level.The cooled compressed air stream that this continuation a indicates enters high-pressure tower 31 in a main heat exchanger 20 downstream part, another part liquefaction in the bath evaporimeter that oxygen enriched liquid (see below) is housed or bath condenser (Badkondensator) 34.A part in this liquefaction portion is sent into medium pressure column 32 by liquid state, and another part is through subcooler 35 and expansion enters lower pressure column 33.
A second compressed air stream l part is passed the passage 24 of main heat exchanger 20 and is cooled to close to dew point in this place.Another part then through one also can be integrated in main heat exchanger 20 heat exchanger assemblies 44 and at this place for evaporating oxygen-rich liquid stream n (see below).Two parts converge once again subsequently and enter medium pressure column 32.
At the bottom of high-pressure tower 31 and medium pressure column 32 tower, extract oxygen coalescence liquid flow respectively, it passes subcooler 35 as stream h and expands and enters lower pressure column 33.
Oxygen-rich liquid stream i is extracted at the bottom of lower pressure column tower, this oxygen-rich liquid stream is by pump 36 raised pressure, lower pressure column central evaporator 37 is imported through expansion valve (non-tag), evaporate at this and nitrogen-enriched stream r (see below) contrary ground part and be imported into the first section 38 of lower pressure column, Qi Tadi is provided with evaporimeter 39 at the bottom of lower pressure column tower.In an embodiment, two condenser/evaporators (lower pressure column central evaporator 37 and lower pressure column tower at the bottom of evaporimeter 39) are configured to falling film evaporator.The liquid state obtained from oxygen column 38 top and gaseous parts are partly fed back to lower pressure column 33 as stream k.The another part flowing out the liquid of the vaporization chamber of lower pressure column central evaporator 37 is sent to lower pressure column first section 38 as withdrawing fluid.
At the bottom of lower pressure column 38 tower, extract liquid oxygen-enriched stream and imported auxiliary condenser 34, this auxiliary condenser is configured to the condenser/evaporator (bath evaporimeter) comprising bath of liquid.Extract gaseous state oxygen-rich stream m from auxiliary condenser 34 top, this gaseous state oxygen-rich stream heated in main heat exchanger 20 and be used to provide gaseous oxygen pressurized product ( sauerstoff-Druckprodukt) (indicate with GOX at this).At the bottom of auxiliary condenser 34 tower, extract liquid oxygen-enriched stream, one shunting n is enhanced pressure in the liquid state, and evaporation in heat exchanger assemblies 44 is also used to provide gaseous oxygen pressurized product equally.Shunting o then part is crossed cold and is used to provide liquid oxygen-enriched air products (indicating with LOX at this) in subcooler 35.This liquid air product can be imported suitable reservoir 61 and be stored in this.
Extract rich nitrogen gaseous flow p from high-pressure tower 31 top and make it liquefy in falling film evaporator or falling film condenser 39.One shunting is fed back to high-pressure tower 31, and another shunting (see bound symbol A), through subcooler 35, is then expanded and entered lower pressure column 33.
Extract rich nitrogen gaseous flow r from medium pressure column 32 top, its part liquefies in falling film evaporator or falling film condenser 37.One shunting is fed back to medium pressure column 32, and s is through subcooler 35 in another shunting, and then demi-inflation enters lower pressure column 33, and part is provided with liquid nitrogen-rich air product (indicating with LIN at this) form.Also can by this liquid nitrogen-rich air product storage in suitable reservoir 62.
Another (larger) of stream r is shunted after t gets around cold compressor 45 under icon first operational mode and is heated in main heat exchanger 20.Another part (the stream u namely in figure) can be extracted by independent hot interchanger 20 at intermediate temperatures, this part subsequently can in " cold " expansion turbine 46 (so-called pressurization nitrogen turbine) swell refrigeration, this expansion turbine such as can couple generator.The part do not expanded in expansion turbine 45 is provided with the form of gaseous state nitrogen-rich air product (indicating with MPGAN at this).After expanding in expansion turbine 45, stream u passes main heat exchanger 20 from cold junction thermotropism end once again and is divided into shunting v and w in the hot side of main heat exchanger 20.Shunting v main air compressor 10 or distribute to this main air compressor purifier in be used as regeneration gas (REGGAS) (see on).Shunting w is then heated by the heat exchanger 51 utilizing hot water stream to run, and then expands in another expansion turbine 52 that can couple generator equally.
Extract nitrogen-enriched stream y from lower pressure column 33 top, in main heat exchanger 20, heat this nitrogen-enriched stream and derived air separation equipment 110.
Because of insulation and main heat exchanger internal loss (the hot side temperature difference) cause, heat leak is inevitable, and as previously mentioned, uses expansion turbine 46 to be to provide the cold therefore and all the time needed if when air separation equipment 110 is in the second operational mode shown in Fig. 2, this cold provided by the liquid air product of institute's feeding, just can disconnect expansion turbine 46.In the illustrated embodiment, its result is that a large amount of corresponding pressurization nitrogen-rich air product is available, therefrom recoverable energy.In other configurations, if such as " directly " is provided by main air compressor and the pressurized stream cooled in main heat exchanger expands in corresponding expansion turbine (being similar to expansion turbine 46), then can reduce the driving power in main air compressor 10.
Fig. 2 illustrates corresponding second operational mode of air separation equipment 110.In this operating mode, on the one hand oxygen-rich liquid air products (LOX) is imported bath evaporimeter or bath condenser 34 (see bound symbol B) from storage tank 61, on the other hand liquid air product (such as from the liquefied air of External liquefying device, indicating with LAIR at this) is sent into lower pressure column 33 from another storage tank 63.Desirably be met because the now chilling requirement of air separation equipment 110 has exceeded, expansion turbine 46 can be disconnected.Thus, according to the extracted amount that gaseous state nitrogen-rich air product (MPGAN) is regulated by valve (non-tag), a large amount of corresponding pressurization nitrogen-rich air product is had (to be also denoted as stream at this x) available, therefrom can to recover energy in expansion turbine 52 or its generator.But must preheated air.But, use corresponding preheating device comparatively to bother.
Cold compressor 45 is also run in the second operating mode.As previously mentioned, liquid air product (in this case LOX and LAIR) will exceed the ice chest of the cold input air separation equipment 110 of needs, causes the Temperature Distribution in heat exchanger " distortion " and the temperature of the stream of one or more outflow heat exchanger is more and more lower.Just air separation equipment reliability service cannot be guaranteed again from a certain limit value.This problem is resolved by cold compressor 45 being run as thermal source in air separation equipment 110.But, cold compressor 45 is not only system heat supply, but by selective compression predetermined substance stream (in this case flow and t) affect and improve overall procedure, this for other heat-producing unit as air heat type, vapor heating type, gas-heated type, electric power hot type heat exchanger or the heat exchanger that otherwise heats can not reach.Boosting effect caused by cold compressor 45 can be utilized in expansion turbine 52.
Compared with the air separation equipment 110 of non-invention, the special beneficial effect of following air separation equipment 100 tool of the present invention, wherein cold compressor 45 is used as so-called feed compressor (Feedverdichter) and is integrated in distillation column system 30.In other words, in the second operating mode, at least one gaseous state pressurized stream (see following each stream b to g) is admitted to cold compressor 45 on the temperature levels of the hot side temperature lower than main heat exchanger 20, is compressed into the second superpressure stress level and on the second superpressure stress level, is admitted at least one destilling tower 31,32 of distillation column system 30 in cold compressor 45 from the first superpressure stress level.In other words, such as one corresponding gaseous state pressurized stream (such as from main air compressor 10 and form is the air of following stream e, or from one of them destilling tower and form is the rich nitrogen state pressurized stream of following stream b to d, f and g) in cold compressor 45, be compressed to one for medium pressure column or high-pressure tower 31 or 32 or the stress level for the tower that take elevated pressures as operating pressure from one for lower pressure column or medium pressure column 32 or 33 or for the stress level of the tower taking lower pressure as operating pressure.In main heat exchanger 20 after corresponding cooling (if being necessary), this compressive flow is sent into corresponding destilling tower 31,32 in correct position place.
Especially for utilizing main compressor 10 to provide the method for the pressurized stream a of two different stress levels and l as this method, this can improve rectification effect.In three-tower system, high-pressure tower 31 should be imported into and the share that must be compressed into the air of high pressure before this diminishes, should medium pressure column be imported into and the share that must be compressed into the air of middle pressure before this then becomes large.Its result is, the total energy consumption of respective air separation equipment 100 significantly reduces.In the case, preferably thus and thus switch cold compressor 45, the joint (pipe joint) of the cold compressor 45 be disconnected in the case is used.This can significantly reduce equipment cost and line cost.
With reference to shown in Fig. 3, the respective air separation equipment 100 according to one embodiment of the present invention is in the second operational mode.Unanimous on the whole shown in first operational mode and Fig. 1, therefore will not again illustrate: in the first operating mode, one flows through expansion turbine 46 accordingly and gets around cold compressor 45.Under the second operational mode as shown in Figure 2, on the one hand oxygen-rich liquid air products (LOX) is imported bath evaporimeter or bath condenser 34 (see bound symbol B) from storage tank 61, on the other hand liquid air product (such as from the liquefied air of External liquefying device, indicating with LAIR at this) is sent into lower pressure column 33 from another storage tank 63.
Cold compressor 45 is at this to extract from the shunting b of the nitrogen-enriched stream y of lower pressure column 33 for charging, therefore this shunting is on the aforementioned superpressure stress level at lower pressure column 33 top, such as 1.3 to 1.4 bar.This shunting b is certainly somebody's turn to do higher (" second ") superpressure stress level that (" first ") superpressure stress level is compressed into the operating pressure equaling medium pressure column 32 in cold compressor 45.Then at intermediate temperatures this compression shunting b is sent into the passage 25 of main heat exchanger 20 and corresponding cooling.After cooling, stream b is sent to medium pressure column 32 top.Other can be shunted j (MPGAN) and z (part is used as regeneration gas REGGAS, optionally only for the first operational mode) when needing equally and derive air separation equipment.The configuration formed by heat exchanger 51 and expansion turbine 52 is used.
With reference to shown in Fig. 4, another air separation equipment according to one embodiment of the present invention is in the second operational mode.Cold compressor 45 also splits into charging to extract from the nitrogen-enriched stream y of lower pressure column 33 at this, and this shunting to indicate with c at this and is on the aforementioned superpressure stress level at lower pressure column 33 top, such as 1.3 to 1.4 bar.This shunting c is certainly somebody's turn to do higher (" second ") superpressure stress level that (" first ") superpressure stress level is compressed into the operating pressure equaling high-pressure tower 31 in cold compressor 45.Then at intermediate temperatures this compression shunting c is sent into the passage 27 of main heat exchanger 20 and corresponding cooling.After cooling, stream c is sent to high-pressure tower 31 top.Other can be flowed j (MPGAN) when needing equally and derive air separation equipment with z (part is used as regeneration gas REGGAS, optionally only for the first operational mode) and rich nitrogen high-pressure spray (HPGAN).
With reference to shown in Fig. 5, another air separation equipment according to one embodiment of the present invention is in the second operational mode.Cold compressor 45 is at this to flow d for charging, and this stream extracts from medium pressure column 32 top, so be on the aforementioned superpressure stress level at medium pressure column 32 top and the temperature levels of medium pressure column.This shunting d is certainly somebody's turn to do higher (" second ") superpressure stress level that (" first ") superpressure stress level is compressed into the operating pressure still equaling high-pressure tower 31 in cold compressor 45.Then at intermediate temperatures this compression shunting d is sent into the respective channel 27 of main heat exchanger 20 and corresponding cooling.After cooling, stream d is sent to high-pressure tower 31 top.Other can be flowed j (MPGAN) when needing equally and derive air separation equipment with z (part is used as regeneration gas REGGAS, optionally only for the first operational mode) and rich nitrogen high-pressure spray (HPGAN).
With reference to shown in Fig. 6, another air separation equipment according to one embodiment of the present invention is in the second operational mode.Cold compressor 45 has been charging from the shunting e of the pressurized stream l of main air compressor 10 since this, and this shunting is on the aforementioned superpressure stress level of the operating pressure equaling medium pressure column 32.The cold junction of independent hot interchanger 20 extracts shunting e, therefore its temperature levels is lower than the hot side temperature levels of main heat exchanger 20.This shunting e is certainly somebody's turn to do higher (" second ") superpressure stress level that (" first ") superpressure stress level is compressed into the operating pressure still equaling high-pressure tower 31 in cold compressor 45.This compression shunting e is then admitted to the passage 21 of main heat exchanger 20 at intermediate temperatures, thus converges with stream a.The stream that this continuation a indicates is by corresponding cooling.A will be flowed after cooling and send into high-pressure tower 31.As mentioned above, other can be flowed j (MPGAN) and z (part is used as regeneration gas REGGAS, optionally only for the first operational mode) when needing equally and derive air separation equipment.
With reference to shown in Fig. 7, another air separation equipment according to one embodiment of the present invention is in the second operational mode.Cold compressor 45 is at this to flow f for charging, and this stream extracts from lower pressure column 33, so on the aforementioned superpressure stress level (such as 1.3 to 1.4 bar) being in lower pressure column 33 and temperature levels thereof.This shunting f is certainly somebody's turn to do higher (" second ") superpressure stress level that (" first ") superpressure stress level is compressed into the operating pressure still equaling medium pressure column 32 in cold compressor 45.This compression shunting f is then admitted to the passage 24 of main heat exchanger 20 at intermediate temperatures, thus converges with stream l.The stream that this continuation l indicates is by corresponding cooling.L will be flowed after cooling and send into medium pressure column 32.As mentioned above, other can be flowed j (MPGAN) and z (part is used as regeneration gas REGGAS, optionally only for the first operational mode) when needing equally and derive air separation equipment.
With reference to shown in Fig. 8, another air separation equipment according to one embodiment of the present invention is in the second operational mode.Cold compressor 45 is at this also to flow g for charging, and this stream extracts from lower pressure column 33, so on the aforementioned superpressure stress level (such as 1.3 to 1.4 bar) being in lower pressure column 33 and temperature levels thereof.This shunting g is certainly somebody's turn to do higher (" second ") superpressure stress level that (" first ") superpressure stress level is compressed into the operating pressure (such as 5.0 to 5.5 bar) still equaling high-pressure tower 31 in cold compressor 45.This compression shunting g is then admitted to the passage 21 of main heat exchanger 20 at intermediate temperatures, thus converges with stream a.The stream that this continuation a indicates is by corresponding cooling.After cooling, stream a is mainly sent into high-pressure tower 31.Other can be flowed j (MPGAN) and z (part is used as regeneration gas REGGAS, optionally only for the first operational mode) when needing equally and derive air separation equipment.
Fig. 9 and Figure 10 is the partial schematic diagram of the possibility arranging cold compressor 45.Corresponding stream no longer uses symbology.All these feasible programs can be realized in all devices shown in Fig. 3 to Fig. 8 and other not shown embodiments of the present invention.
According to Fig. 9, the stream compressed through cold compressor 45 is admitted to main heat exchanger 20 in hot side.With reference to shown in Figure 10, under the first medium temperature, independent hot interchanger 20 extracts first-class, then compresses this stream and under the second medium temperature, it is sent into main heat exchanger 20 once again.

Claims (14)

1. the method for production at least one air products, wherein use air separation equipment (100), this air separation equipment has main air compressor (10), main heat exchanger (20) and distillation column system (30), this distillation column system comprises high-pressure tower (31), medium pressure column (32), lower pressure column (33), evaporimeter (39) at the bottom of lower pressure column tower and lower pressure column central evaporator (37), wherein this high-pressure tower (31) runs with the operating pressure higher than this lower pressure column (33), this medium pressure column (32) runs with the operating pressure between this high-pressure tower (31) and the operating pressure of this lower pressure column (33), and evaporimeter (39) at the bottom of this lower pressure column tower and this lower pressure column central evaporator (37) are configured to condenser/evaporator, it is characterized in that, the method comprises the first operational mode and the second operational mode, wherein
-in the first operating mode, store the liquid air product (LIN, LOX) that at least one produces in this distillation column system (30), and
-in the second operating mode,
Other liquid air product (LIN, LOX, the LAIR) of-liquid air product (LIN, LOX, LAIR) that at least one stored in the first operating mode and/or at least one is sent in this distillation column system (30), and
-at least one gaseous state pressurized stream (b-g) cold compressor (45) will be sent at the temperature levels of the hot side temperature lower than this main heat exchanger (20), the second superpressure stress level is compressed to by the first superpressure stress level in this cold compressor (45), and send at least in part at least one destilling tower (31,32) of this distillation column system (30) at this second stress level.
2. method according to claim 1, wherein in the first operating mode, at least one pressurized stream and/or at least one other gaseous state pressurized stream (b-g) swell refrigeration in expansion turbine (46).
3. according to the method for claim 1 or 2, wherein from this lower pressure column (33,38) evaporation is to provide gaseous oxygen pressurized product (GOX) in auxiliary condenser (34) for the oxygen coalescence stream at the bottom of tower, and wherein this auxiliary condenser (34) is configured to condenser/evaporator.
4. according to the method for one of claims 1 to 3, wherein this first stress level is equivalent to the operating pressure of this lower pressure column (33), and/or this second stress level is equivalent to the operating pressure of this high-pressure tower (31).
5. according to the method for one of Claims 1-4, wherein this first stress level is equivalent to the operating pressure of this lower pressure column (33) and this second stress level is equivalent to the operating pressure of this medium pressure column (32) or this high-pressure tower (31), or this first stress level is equivalent to the operating pressure of this medium pressure column (32) and this second stress level is equivalent to the operating pressure of this high-pressure tower (31).
6. according to the method for one of aforementioned claim, wherein at least one gaseous state pressurized stream (b-d, f, g) be being formed at least partially of the stream of being discharged by the destilling tower (32,33) run as operating pressure using this first stress level of this distillation column system (30).
7. according to the method for one of claim 1 to 6, wherein this at least one gaseous state pressurized stream (e) be being formed at least partially by the stream utilizing this main air compressor (10) to provide and utilize this main heat exchanger (20) to cool.
8. according to the method for one of aforementioned claim, wherein this at least one gaseous state pressurized stream (e) converged at this second stress level and at least one other stream (a) before at least one destilling tower (31,32) being admitted to this distillation column system (30).
9. according to the method for one of aforementioned claim, wherein this at least one gaseous state pressurized stream (a-g) cooling in this main heat exchanger (20) at least in part after compression in this cold compressor (45).
10. method according to claim 9, wherein this at least one gaseous state pressurized stream (a-g) send into this main heat exchanger (20) to cool in hot side or at the temperature levels of other the hot side temperature lower than this main heat exchanger (20) after compression in this cold compressor (45).
11. according to the method for one of aforementioned claim, a wherein part for the gaseous state pressurized stream (a-g) of compression heating and/or derived by this air separation equipment (100) at least in part in this main heat exchanger (20) in this cold compressor (45).
12. air separation equipments (100), it has main air compressor (10), main heat exchanger (20) and distillation column system (30) and set up to run under the first operational mode and the second operational mode, wherein be provided with the liquid air product (LIN produced in this distillation column system (30) to store at least one in the first operating mode, LOX) the liquid air product (LIN and in the second operating mode at least one stored in the first operating mode, LOX, and/or other liquid air product (LIN of at least one LAIR), LOX, LAIR) device (61-63) set up in this distillation column system (30) is sent into, it is characterized in that, this air separation equipment (100) comprises cold compressor (45), and be provided with in the second operating mode at least one gaseous state pressurized stream (b-g) be sent into this cold compressor (45) at the temperature levels of the hot side temperature lower than this main heat exchanger (20), in this cold compressor (45), be compressed to the second superpressure stress level by the first superpressure stress level and send at least one destilling tower (31 of this distillation column system (30) subsequently at this second stress level at least in part, 32) device set up in.
The method of 13. generation electric energy, wherein at least provides at least one air products by according to the method for one of claim 1 to 11 during the second operational mode, and uses it for generation and/or transform at least one fuel.
14. in order to implement method according to claim 13, especially in order to implement oxygen-rich combustion method and/or integrated gasification combined cycle plants method and the equipment set up.
CN201480039508.0A 2013-07-11 2014-07-10 Produce method, the air separation plant, the method and apparatus produced electricl energy of at least one air products Active CN105378411B (en)

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