US20210348839A1 - System and method for cryogenic air separation using a booster loaded liquid turbine for expansion of a liquid air stream - Google Patents
System and method for cryogenic air separation using a booster loaded liquid turbine for expansion of a liquid air stream Download PDFInfo
- Publication number
- US20210348839A1 US20210348839A1 US17/126,220 US202017126220A US2021348839A1 US 20210348839 A1 US20210348839 A1 US 20210348839A1 US 202017126220 A US202017126220 A US 202017126220A US 2021348839 A1 US2021348839 A1 US 2021348839A1
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- US
- United States
- Prior art keywords
- air stream
- bar
- pressure
- compressed
- booster compressor
- Prior art date
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- 229910052757 nitrogen Inorganic materials 0.000 claims description 31
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- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 7
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- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
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- 238000001179 sorption measurement Methods 0.000 description 1
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Images
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- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
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- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04D—NON-POSITIVE-DISPLACEMENT PUMPS
- F04D17/00—Radial-flow pumps, e.g. centrifugal pumps; Helico-centrifugal pumps
- F04D17/08—Centrifugal pumps
- F04D17/10—Centrifugal pumps for compressing or evacuating
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04D—NON-POSITIVE-DISPLACEMENT PUMPS
- F04D25/00—Pumping installations or systems
- F04D25/02—Units comprising pumps and their driving means
- F04D25/04—Units comprising pumps and their driving means the pump being fluid-driven
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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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
- F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air
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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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
- F25J2240/12—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
- F25J2240/20—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being oxygen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/30—Dynamic liquid or hydraulic expansion with extraction of work, e.g. single phase or two-phase turbine
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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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
- F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air
Definitions
- the present invention relates to a system and method of cryogenic air separation, and more particularly to cryogenic air separation that employs the use of a booster-loaded liquid turbine for the expansion of a liquid air stream and the associated recovery of work therefrom.
- Liquid turbines or dense phase turbines are currently used in high pressure air separation units to extract work from the liquid air stream or supercritical air stream that has been condensed against boiling product oxygen or against some product nitrogen from the air separation unit.
- This air stream is typically compressed to elevated pressures in order to effectively boil the product(s) but is subsequently expanded prior to introduction to the distillation columns of the air separation units.
- Such liquid turbines tend to be used in either nitrogen liquefaction applications (e.g. less than 400 tons per day of liquid nitrogen product) typically with an oil brake coupled to the liquid turbine for dissipating the extracted power or in large volume air separation units (e.g. greater than about 2000 tons per day of oxygen product) and typically with a fixed speed generator coupled to the liquid turbine for recovery of power.
- nitrogen liquefaction applications e.g. less than 400 tons per day of liquid nitrogen product
- large volume air separation units e.g. greater than about 2000 tons per day of oxygen product
- a fixed speed generator coupled to the liquid turbine for recovery of power.
- liquid turbines or dense phase turbines generally improve the performance of the air separation unit but involve additional capital costs for the liquid turbine, generator, and associated controls. Because of the additional capital costs associated with the installation and use of the liquid turbine, generator, and associated controls, liquid turbines are currently deemed beneficial only in larger cryogenic air separation units.
- Booster loaded liquid turbines are generally avoided in cryogenic air separation plants because most of the streams available to boost, such as the boiler air stream or other feed air stream upstream of the heat exchanger are gas streams, and there is an inherent aerodynamic and speed mismatch in coupling a booster stage for these gas streams with a turbine handling a fluid of liquid-like density. This inherent aerodynamic and speed mismatch will tend to result in lower efficiencies, and in some cases perhaps even the inability to design a viable turbine-booster pairing.
- the present invention may be characterized as an air separation unit having a booster loaded liquid turbine arrangement configured to produce one or more oxygen enriched streams and one or more nitrogen enriched streams, the air separation unit comprising: (i) a main air compression system configured to receive an incoming air stream and produce a compressed air stream at a pressure of between about 5 bar(a) and 15 bar(a); (ii) a pre-purification unit configured to pre-purify the compressed air stream to produce a compressed, pre-purified air stream; (iii) a primary booster compressor configured to receive a portion of the compressed, pre-purified air stream and produce a further compressed, pre-purified air stream at a pressure of between about 25 bar(a) and 90 bar(a); (iv) a supplemental booster compressor configured to further compress the further compressed, pre-purified air stream and produce a still further compressed, pre-purified air stream at a pressure of between about 30 bar(a) and 95 bar(a); (v) a main heat exchanger configured to cool the still further compressed, pre-
- the present invention may also be characterized as a method for cryogenic air separation comprising the steps of: (a) compressing an incoming air stream in a main air compression system configured to a pressure of between about 5 bar(a) and 15 bar(a); (b) pre-purifying the compressed air stream to produce a compressed, pre-purified air stream; (c) further compressing all or a portion of the compressed, pre-purified air stream in a primary booster compressor to produce a further compressed, pre-purified air stream at a pressure of between about 25 bar(a) and 90 bar(a); (d) still further compressing the further compressed, pre-purified air stream in a supplemental booster compressor to produce a still further compressed, pre-purified air stream at a pressure of between about 30 bar(a) and 95 bar(a); (e) cooling the still further compressed, pre-purified air stream in a main heat exchanger to produce a liquid air stream; (f) expanding the liquid air stream in a liquid turbine operatively coupled to the supplemental booster compressor to produce an expanded
- the supplemental booster compressor may be a cold booster compressor configured to receive the further compressed, pre-purified air stream, preferably at a pressure of between about 40 bar(a) and 50 bar(a) that has been partially cooled in the main heat exchanger and produce a still further compressed, pre-purified air stream at a pressure of preferably between about 50 bar(a) and 60 bar(a).
- the supplemental booster compressor may be a warm booster compressor configured to further compress the further compressed, pre-purified air stream, preferably at a pressure of between about 70 bar(a) and 90 bar(a) and before any cooling in the main heat exchanger. The warm supplemental booster compressor then produces a still further compressed, pre-purified air stream at a pressure of preferably between about 75 bar(a) and 95 bar(a).
- the portion of the compressed, pre-purified air stream received by the primary booster compressor in the present air separation unit and associated methods is preferably a boiler air stream comprising between about 25% to 45% by volume of the incoming compressed, pre-purified air stream.
- the expanded air stream is directed to the higher pressure column of the distillation column system, whereas in other embodiments a first portion of the expanded air stream is directed to the higher pressure column of the distillation column system and a second portion of the expanded air stream is further reduced in pressure with an expansion valve and directed to the lower pressure column of the distillation column system.
- FIG. 1 is a schematic diagram of a cryogenic air separation unit with a conventional generator loaded liquid turbine commonly used in the prior art
- FIG. 2 is a schematic diagram of a cryogenic air separation unit having a warm booster loaded liquid turbine in accordance with an embodiment of the present system and method for cryogenic air separation;
- FIG. 3 is an illustration of an example of a booster loaded liquid turbine used in the embodiment of FIG. 2 ;
- FIG. 4 is a schematic diagram of a cryogenic air separation unit with a cold booster loaded liquid turbine in accordance with another embodiment of the present system and method for cryogenic air separation;
- FIG. 5 is a graph showing data from computer simulations showing the total net compression power versus the fraction of the incoming air stream directed to the boiler air stream and comparing the prior art generated loaded liquid turbine to embodiments of a booster loaded liquid turbine.
- FIG. 1 a prior art cryogenic air separation unit 10 employing a generator loaded liquid turbine 50 is illustrated.
- FIG. 2 and FIG. 4 illustrate embodiments of a cryogenic air separation unit 110 , 210 employing a booster-loaded loaded liquid turbine 150 , 250 .
- Cryogenic air separation units 10 . 110 , 210 are each configured to receive an incoming feed air stream 12 and produce a plurality of product streams and/or waste streams that optionally include a high pressure gaseous oxygen stream 102 , a low pressure gaseous oxygen stream 104 , a liquid oxygen stream 95 , a liquid nitrogen product stream 90 , a plurality of gaseous nitrogen enriched streams 101 , 106 , 108 , and a crude argon stream 63 .
- Production of the streams is preferably achieved via use of a triple column fractional distillation process.
- the depicted air separation units 10 , 110 , and 210 all include a main feed air compression train, a turbine air circuit, a boiler air circuit; a main or primary heat exchanger 60 ; and a distillation column system 70 .
- the incoming feed air streams 12 is typically drawn through an air suction filter house (not shown) and compressed in a multi-stage, intercooled main air compressor arrangement 20 to a pressure that can be between about 5 bar(a) and about 15 bar(a).
- This main air compressor arrangement 20 may include integrally geared compressor stages or a direct drive compressor stages, arranged in series or in parallel.
- the compressed air stream 14 exiting the respective main air compressor arrangement 20 is fed to an aftercooler with or without integral demister to remove the free moisture in the incoming feed air stream.
- the cool, compressed air feed 14 is then purified in a pre-purification unit 25 to remove high boiling contaminants from the cool, compressed air feed.
- the pre-purification unit 25 typically contains two beds or more of alumina and/or molecular sieve operating in accordance with a temperature and/or pressure swing adsorption cycle in which moisture and other impurities, such as carbon dioxide, water vapor and hydrocarbons, are adsorbed. While one of the beds is used for pre-purification of the cool, dry compressed air feed while the other bed is regenerated, preferably with a portion of the waste nitrogen from the air separation unit.
- the two beds switch service periodically. Particulates are subsequently removed from the compressed, pre-purified feed air in a dust filter disposed downstream of the pre-purification unit 25 to produce the compressed, purified air streams 28 .
- the compressed and purified air stream 28 is separated into oxygen-rich, nitrogen-rich, and argon-rich fractions in a plurality of distillation columns including a higher pressure column 72 ; a lower pressure column 74 ; and an argon column arrangement, which may include an argon column 76 .
- the compressed and pre-purified air streams 28 is typically split into a plurality of feed air streams, which includes at least a boiler air stream 42 and a turbine air stream 32 .
- the boiler air stream 42 comprises generally between about 25% to 45% of the compressed and purified feed air stream 28 .
- the boiler air streams 42 may be further compressed in a booster compressor arrangement 44 to a targeted pressure between about 25 bar(a) and about 90 bar(a) and subsequently cooled in aftercooler (not shown) to form a boosted pressure air stream 45 .
- the target pressure of the boosted pressure air streams 45 is generally dictated by the product requirements for the high pressure gaseous oxygen product stream 102 .
- the boosted pressure air stream 45 is then further cooled to temperatures required for rectification in the main heat exchanger 60 where it is used to boil liquid oxygen streams 97 via indirect heat exchange to produce the high pressure gaseous oxygen product stream 102 and/or a low pressure gaseous oxygen product stream 104 .
- the cooled and further compressed boiler air streams 46 exiting main heat exchanger 60 is often a liquid air stream or other dense phase fluid which is expanded in liquid turbine 50 (See FIG. 1 ) operatively coupled to a generator system 52 .
- liquid air stream or other dense phase fluid which is expanded in liquid turbine 150 is coupled to a warm booster compressor 121 while in the embodiment shown in FIG. 4 the liquid air stream or other dense phase fluid which is expanded in liquid turbine 150 is coupled to a cold booster compressor 221 .
- the expanded streams 47 exiting the liquid turbines 50 , 150 , 250 are divided into two separate portions and introduced into the higher pressure column 72 and the lower pressure column 74 of the distillation column system 70 .
- the portion of the expanded stream 47 directed to the lower pressure column 74 may be further reduced in pressure via expansion valve 48 yielding a low pressure air stream 49 for introduction into the lower pressure column 74 .
- the turbine air stream 32 is generally about 55% to 75% of the compressed and purified feed air stream 28 and is optionally further compressed in one or more turbine air compressors 33 , cooled in an aftercooler and then directed as stream 34 to the main heat exchanger 60 where it is partially cooled prior to being directed to a turbine based refrigeration circuit that includes a turboexpander 36 as described below.
- the target pressure of the further compressed turbine air stream 35 is preferably between about 20 bar(a) and about 60 bar(a).
- the partially cooled feed air stream 35 is expanded in turboexpander 36 to an exhaust stream 38 that is directed to the higher pressure column 72 or lower pressure column 74 of the distillation column system 70 . In the illustrated embodiment, the exhaust stream 38 is shown directed to the higher pressure column 72 .
- liquid production in the cryogenic air separation units may be further varied by varying the pressure in the turbine air stream sent to the turboexpander.
- This variation in pressure can be effectuated by a turbine air stream bypass circuit (not shown) which includes a bypass line having a bypass valve that can be set in an open or closed position.
- the bypass circuit is configured to direct all or a portion of the turbine air stream to bypass at least one of the one or more turbine air compressors. If a bypass circuit is employed, the target pressure of the bypassed turbine air stream is preferably between about 10 bar(a) and about 30 bar(a). Also, in some embodiments that utilize the bypass circuit, it may be advantageous to provide a source of make-up nitrogen that is directed to the turbine air stream compressors in lieu of the turbine air stream so as to not damage the turbine air compressor.
- the main or primary heat exchanger 60 is preferably a brazed aluminum plate-fin type heat exchanger. Such heat exchangers are advantageous due to their compact design, high heat transfer rates and their ability to process multiple streams. They are manufactured as fully brazed and welded pressure vessels. For small air separation unit units, a heat exchanger comprising a single core may be sufficient. For larger air separation unit units handling higher air flows, the main heat exchanger may be constructed from several heat exchange cores which may be divided into high pressure cores and low pressure cores.
- the components of the feed air stream namely oxygen, nitrogen, and argon are separated within the distillation column system 70 that preferably includes a plurality of distillation columns in which vapor and liquid are counter-currently contacted in order to produce a gas/liquid mass-transfer based separation of the respective feed streams.
- Such columns will preferably employ structured packing or trays as the mass transfer contacting elements.
- the illustrated distillation column system 70 includes: a higher pressure column 72 typically configured to operate in the range from between about 20 bar(a) to about 60 bar(a); a lower pressure column 74 typically configured to operate in the range from between about 1.1 bar(a) to about 1.5 bar(a); a main condenser-reboiler 75 ; and an argon column arrangement.
- the illustrated argon column arrangement preferably is configured as an argon superstaged or ultra superstaged column 76 with an argon condenser 77 disposed in a separate shell 78 .
- the higher pressure column 72 and the lower pressure column 74 are preferably inked in a heat transfer relationship such that a portion of the nitrogen-rich vapor column overhead, extracted from proximate the top of higher pressure columns 72 as a stream 88 is condensed within the condenser-reboiler 75 typically located in the base of lower pressure column 74 against boiling an oxygen-rich liquid column bottoms 92 .
- the boiling of oxygen-rich liquid column bottoms 92 initiates the formation of an ascending vapor phase within lower pressure columns 74 .
- the condensation produces a liquid nitrogen rich stream 86 that may be divided into a reflux stream 87 that refluxes one or more of the distillation columns to initiate the formation of the descending liquid phase and a shelf nitrogen stream 89 that may be subcooled in heat exchanger 55 and taken as a liquid nitrogen product stream 90 . Also, another portion of the nitrogen-rich vapor column overhead from the higher pressure column 72 may be taken and warmed in the main heat exchanger 60 to produce a high pressure gaseous nitrogen stream 101 .
- a portion of the expanded air stream 47 exiting the liquid turbine is introduced into the higher pressure column 72 for distillation by contacting an ascending vapor phase of such mixture within a plurality of mass transfer contacting elements which may comprise trays or structured packing, with a descending liquid phase that is initiated by the reflux streams.
- This distillation process produces crude liquid oxygen column bottoms 82 also known as kettle liquid, and a high pressure nitrogen-rich column overhead.
- a portion of the expanded air stream 47 exiting the liquid turbine is further reduced in pressure by the expansion valve 148 and introduced into the lower pressure column 74 for distillation.
- the separation occurring within lower pressure column 74 produces a nitrogen-rich vapor column overhead that is extracted as a low pressure nitrogen stream 58 and a low pressure nitrogen waste stream 56 .
- the separation further yields an oxygen-rich liquid column bottoms 92 , a portion of which may be extracted from the lower pressure column 74 as an oxygen-rich liquid stream 94 .
- a portion of the oxygen-rich liquid stream 94 may be pumped via pump 96 to yield a pumped liquid oxygen stream 97 which is directed to the associated main heat exchanger 60 .
- a first portion of the pumped liquid oxygen stream 97 is warmed to produce a high pressure gaseous oxygen product stream 102 , while a second portion is reduced in pressure via valve 98 and the resulting lower pressure oxygen stream 99 is then warmed in main heat exchanger 60 to produce a low pressure oxygen product stream 104 .
- Another portion of the oxygen-rich liquid stream 94 taken from the lower pressure column 74 may be taken as a liquid oxygen product stream 95 .
- nitrogen waste streams 106 may also be extracted from lower pressure column 74 to control the purity of the low pressure nitrogen product streams 108 .
- the low pressure nitrogen product stream 58 and the nitrogen waste stream 56 are preferably passed through one or more subcooling units 55 designed to subcool: (i) the liquid nitrogen product stream 89 ; and (ii) the respective kettle streams 186 , 286 used to reflux the argon column 76 .
- the argon column arrangement is configured to receive an oxygen-rich stream 62 typically having a concentration of about 8% to 15% by volume argon from an intermediate location of the lower pressure column 74 and separate argon and oxygen using the oxygen-rich stream 62 as an ascending vapor stream against a downflowing argon-rich reflux stream 67 received from an argon condenser 77 .
- the mass transfer contacting elements within the argon column arrangement could be trays or structured packing.
- the resulting argon-rich vapor overhead stream 65 from the argon column 76 is then preferably directed to the argon condenser 77 where the argon-rich vapor overhead stream is condensed into a crude liquid argon stream 66 .
- a first portion of the crude liquid argon stream 66 is used as the argon-rich reflux stream 67 and the remaining portion of the crude liquid argon 66 taken as a crude argon stream 63 .
- the oxygen rich column bottoms stream 64 from the argon column 76 is preferably returned to the lower pressure column.
- the cooling duty of the argon condenser 77 is provided via a subcooled stream 85 of the oxygen-enriched stream 84 taken from the kettle liquid 82 of the higher pressure column 72 .
- the vaporized portion 68 of the condensing media as well as a portion of the excess liquid in the bottom of the shell 78 may be returned to the lower pressure column 74 as stream 69 .
- the argon condenser 77 may be configured as a conventional argon condenser or as a down-flowing once-through argon condenser and is preferably disposed in a separate shell 78 or alternatively disposed within the lower pressure column 74 .
- FIG. 2 the differences between the illustrated warm booster loaded liquid turbine and the prior art generator-loaded liquid turbine of FIG. 1 include: a booster loaded liquid turbine 150 ; a warm booster bypass circuit; and a liquid turbine bypass circuit. Details of the warm booster loaded liquid turbine (i.e. liquid turbine 150 that is operatively coupled to a discrete warm booster compressor 121 ) is discussed below and with reference to the discussion of FIG. 3 .
- the warm booster bypass circuit comprises an air circuit that includes a diversion valve 123 configured to allow the further compressed boiler air stream 122 to bypass the warm booster compressor 121 and send the further compressed boiler air stream 122 directly to the main heat exchanger 60 during air separation unit start-up operation and other operating conditions where the liquid turbine is off-line.
- the diversion valve 123 is closed, the further compressed boiler air stream 122 will be still further compressed in warm booster compressor circuit that includes the warm booster compressor 121 and a recirculation valve 124 as well as the control valve 126 .
- the further compressed boiler air stream 122 is directed to the warm booster compressor 121 .
- the still further compressed boiler air stream 128 is recirculated back upstream of the warm booster compressor 121 via an open recirculation valve 124 (with control valve 126 in ‘closed’ position) or the still further compressed boiler air stream 128 is directed to the main heat exchanger 60 via the open control valve 126 (with the recirculation valve 124 in ‘closed’ position).
- the control valve 126 is ‘open’ then recirculation valve 124 and diversion valve 123 are ‘closed’.
- the diversion valve 123 is ‘open’ then recirculation valve 124 and control valve 126 are ‘closed’.
- the liquid turbine bypass circuit includes bypass valve 153 that directs cooled compressed, boiler air stream 146 to the higher pressure column 72 while bypassing the liquid turbine circuit.
- the liquid turbine circuit preferably comprises valve 151 , liquid turbine 150 , and valve 152 which directs the resulting expanded air stream 154 to the higher pressure column 72 .
- the liquid turbine 150 is generally bypassed concurrently with bypassing the warm booster compressor 121 .
- bypass valve 153 is set in the ‘open’ position while valves 151 and 152 are set in the ‘closed’ position.
- the required discharge pressure of the primary boiler air compressor 144 would be lower thereby reducing the operating costs associated with the primary boiler air compressor 144 .
- Such net higher pressure of the boiler air stream 145 translates to improved performance of the air separation unit 110 , 210 in in the form of additional refrigeration capacity and/or power savings during operation of the air separation unit 110 , 210 as more of the incoming air flow 12 can be directed to the turbine air circuit and less of the incoming air flow 12 to the boiler air circuit.
- there would be a capital cost savings by avoiding the capital costs associated with the generator and associated controls, partially offset by the added costs of the booster loaded liquid turbine arrangement.
- booster loaded liquid turbine 500 that employs an advanced aerodynamic design similar to other booster loaded gas turbine chassis.
- one embodiment of the booster loaded liquid turbine 500 includes a rotor assembly 510 , a plurality of active magnetic bearings 520 , 530 and a plurality of seals including a seal 540 disposed between the rotor assembly 510 and the liquid turbine 150 as well as a seal 550 disposed between the rotor assembly and the warm compressor 121 .
- the size of the liquid or dense phase turbine 150 and the coupled compressor 121 are relatively small such that there is an aerodynamic and speed match between the turbine and the coupled gas compressor.
- the pressure ratio across the dedicated warm booster compressor is preferably only about 1.1 or less, as shown in the Example of FIG. 3 with the incoming purified, compressed air being at 1150 psia and the further compressed air stream exiting the warm booster compressor 121 being about 1250 psia.
- use of an aftercooler to cool the further compressed stream is optional and is preferably avoided to further reduce capital and operating costs.
- the incoming liquid or dense phase fluid is at 1250 psia and expanded to an exhaust stream of roughly 100 psia.
- the recovered work of the expansion of the fluid having liquid-like densities in turbine 150 is transferred to the warm booster compressor 121 via rotor assembly 510 .
- FIG. 4 shows a schematic diagram of a cryogenic air separation unit having a booster loaded liquid turbine 250 coupled to a cold-compressor 221 .
- the booster loaded liquid turbine is used for cold compression of all or a portion of the boiler air stream that was introduced into the main heat exchanger.
- the air separation unit of FIG. 4 is similar to that of the air separation unit of FIG. 2 except that the dedicated booster compressor is a cold compressor in lieu of the warm compressor shown in FIG. 2 .
- the differences between the illustrated cold booster loaded liquid turbine in FIG. 4 and the prior art generator-loaded liquid turbine of FIG. 1 include: a liquid turbine 250 that is operatively coupled to a cold booster compressor 221 ; a cold booster bypass circuit; and a liquid turbine bypass circuit.
- the boiler air stream 142 in the boiler air circuit is compressed to a certain design pressure by the primary boiler air compressor 144 and then directed to the main heat exchanger 60 .
- the cold booster bypass circuit comprises an air circuit that includes a bypass valve 223 configured to allow the further compressed boiler air stream 145 to bypass the cold booster compressor 221 and proceed through the main heat exchanger 60 directly to the higher pressure column 72 during air separation unit operating conditions where the liquid turbine is off-line.
- the compressed boiler air stream 145 will be withdrawn from the main heat exchanger 60 at an intermediate location and directed to the cold booster compressor 221 via control valve 226 .
- the intermediate location of the main heat exchanger 60 generally corresponds to the location where the temperature of the boiler air stream 222 is near the boiling temperature for subcritical boiling applications.
- the further compressed stream 228 exiting the cold booster compressor 221 is then re-introduced to the main heat exchanger 60 for product boiling purposes and to the higher pressure column 72 .
- the liquid turbine bypass circuit includes bypass valve 253 that directs cooled compressed, boiler air stream 146 to the higher pressure column 172 while bypassing the liquid turbine circuit.
- the liquid turbine circuit preferably comprises valve 251 , liquid turbine 250 , and valve 252 which directs the resulting expanded air stream 254 to the higher pressure column 172 .
- the liquid turbine 250 is generally bypassed concurrently with bypassing the cold booster compressor 221 .
- bypass valve 253 is set in the ‘open’ position while valves 251 and 252 are set in the ‘closed’ position.
- the pressure ratio across the dedicated cold booster compressor may be higher than the pressure ratio across the dedicated warm booster compressor in the embodiment of FIG. 2 while still maintaining the aerodynamic and speed match between the turbine and the coupled gas compressor.
- the pressure ratio across the cold compressor was about 1.15 enabling the air separation unit to operate with a lower inlet boiler air pressure which provides further power savings compared to the warm booster compression arrangement depicted in FIG. 2 .
- Such net higher pressure of the boiler air stream translates to improved performance of the air separation unit in in the form of additional refrigeration capacity and/or power savings during operation of the air separation unit as more of the incoming air flow can be directed to the turbine air circuit and less of the incoming air flow to the boiler air circuit.
- computer modeling suggests that using the cold booster loaded liquid turbine arrangement of FIG. 4 yields a power savings of about 1.8% compared to a comparably sized air separation unit without the booster loaded liquid turbine, shown generally in FIG. 1 .
- FIG. 5 there is shown a graph plotting selected results of the simulations, and particularly the expected total net compression power consumed versus the fraction of the incoming air stream directed to the boiler air stream for comparably sized cryogenic air separation units.
- the first curve 610 on the graph represents the simulation data for a cryogenic air separation unit having a generated loaded liquid turbine with the primary boiler air compressor is configured to raise the pressure of the boiler air stream to about 1200 psia.
- the second curve 620 on the graph represents the simulation data for a cryogenic air separation unit having an embodiment of a booster loaded liquid turbine wherein the primary boiler air compressor is configured to raise the pressure of the boiler air stream to only about 1100 psia and the supplemental booster compressor is configured further compress the boiler air stream to a pressure of about 1200 psia. Note the pressure of the boiler air stream exiting the primary boiler air compressor is lower than the baseline case of a cryogenic air separation unit having a generator loaded liquid turbine. Comparing the first curve 610 to the second curve 620 , one would notice there is a small power penalty incurred when the booster-loaded liquid turbine is used compared to the generated-loaded liquid turbine at the same boiler air pressure.
- the third curve 630 on the graph of FIG. 5 represents the simulation data for a cryogenic air separation unit having a booster loaded liquid turbine wherein the primary boiler air compressor is configured to raise the pressure of the boiler air stream to about 1200 psia—which is comparable to the pressure of the boiler air stream exiting the primary boiler air compressor in the baseline case—and the supplemental booster compressor is configured to further compress the boiler air stream to a pressure of about 1295 psia.
- Such an application may be used in retrofit situations of pre-existing air separation units to
- the beneficial effect of raising the boiler air stream pressure from 1200 psia exiting the primary boiler air compressor to 1,295 psia exiting the supplemental booster compressor (as represented by curve 630 ) in an upper column turbine cycle means less turbine air stream flow is required to produce the same or similar product slates while using less overall net compression power in the main air compressor (MAC).
- MAC main air compressor
- pressure enhancement may allow the same air separation unit to realize better oxygen recovery and/or less incoming feed airflow.
- the present system and method for cryogenic air separation units using a booster-loaded liquid turbine may also be used in air separation units where a generator-loaded liquid turbine arrangement is deemed economically unfavorable.
- the following table presents results of computer simulations comparing a cryogenic air separation project without the booster-loaded liquid turbine arrangement compared to a cryogenic air separation project with the booster-loaded liquid turbine arrangement having a cold booster compressor.
Abstract
Description
- This application claims the benefit of and priority to U.S. provisional patent application Ser. No. 63/020,045 filed May 5, 2020 the disclosure of which is incorporated by reference.
- The present invention relates to a system and method of cryogenic air separation, and more particularly to cryogenic air separation that employs the use of a booster-loaded liquid turbine for the expansion of a liquid air stream and the associated recovery of work therefrom.
- Liquid turbines or dense phase turbines are currently used in high pressure air separation units to extract work from the liquid air stream or supercritical air stream that has been condensed against boiling product oxygen or against some product nitrogen from the air separation unit. This air stream is typically compressed to elevated pressures in order to effectively boil the product(s) but is subsequently expanded prior to introduction to the distillation columns of the air separation units.
- Such liquid turbines tend to be used in either nitrogen liquefaction applications (e.g. less than 400 tons per day of liquid nitrogen product) typically with an oil brake coupled to the liquid turbine for dissipating the extracted power or in large volume air separation units (e.g. greater than about 2000 tons per day of oxygen product) and typically with a fixed speed generator coupled to the liquid turbine for recovery of power. When used, such liquid turbines or dense phase turbines generally improve the performance of the air separation unit but involve additional capital costs for the liquid turbine, generator, and associated controls. Because of the additional capital costs associated with the installation and use of the liquid turbine, generator, and associated controls, liquid turbines are currently deemed beneficial only in larger cryogenic air separation units.
- Booster loaded liquid turbines are generally avoided in cryogenic air separation plants because most of the streams available to boost, such as the boiler air stream or other feed air stream upstream of the heat exchanger are gas streams, and there is an inherent aerodynamic and speed mismatch in coupling a booster stage for these gas streams with a turbine handling a fluid of liquid-like density. This inherent aerodynamic and speed mismatch will tend to result in lower efficiencies, and in some cases perhaps even the inability to design a viable turbine-booster pairing.
- What is needed is a liquid turbine arrangement that has reduced capital costs compared to conventional generator-loaded liquid turbine arrangements but still yields improved performance of the air separation unit in the form of additional refrigeration and/or power savings during operation of the air separation unit.
- The present invention may be characterized as an air separation unit having a booster loaded liquid turbine arrangement configured to produce one or more oxygen enriched streams and one or more nitrogen enriched streams, the air separation unit comprising: (i) a main air compression system configured to receive an incoming air stream and produce a compressed air stream at a pressure of between about 5 bar(a) and 15 bar(a); (ii) a pre-purification unit configured to pre-purify the compressed air stream to produce a compressed, pre-purified air stream; (iii) a primary booster compressor configured to receive a portion of the compressed, pre-purified air stream and produce a further compressed, pre-purified air stream at a pressure of between about 25 bar(a) and 90 bar(a); (iv) a supplemental booster compressor configured to further compress the further compressed, pre-purified air stream and produce a still further compressed, pre-purified air stream at a pressure of between about 30 bar(a) and 95 bar(a); (v) a main heat exchanger configured to cool the still further compressed, pre-purified air stream to produce a liquid air stream; (vi) a liquid turbine operatively coupled to the supplemental booster compressor and configured to expand the liquid air stream and produce an expanded air stream at a pressure between 7 bar(a) and 12 bar(a) and wherein the work of expansion is used to drive the supplemental booster compressor; and (vii) a distillation column system comprising a higher pressure column and a lower pressure column linked in a heat transfer relationship via a condenser reboiler, the distillation column system configured to receive all or a portion of the expanded air stream in the higher pressure column for distillation of the expanded air stream into the one or more oxygen enriched streams and the one or more nitrogen enriched streams.
- The present invention may also be characterized as a method for cryogenic air separation comprising the steps of: (a) compressing an incoming air stream in a main air compression system configured to a pressure of between about 5 bar(a) and 15 bar(a); (b) pre-purifying the compressed air stream to produce a compressed, pre-purified air stream; (c) further compressing all or a portion of the compressed, pre-purified air stream in a primary booster compressor to produce a further compressed, pre-purified air stream at a pressure of between about 25 bar(a) and 90 bar(a); (d) still further compressing the further compressed, pre-purified air stream in a supplemental booster compressor to produce a still further compressed, pre-purified air stream at a pressure of between about 30 bar(a) and 95 bar(a); (e) cooling the still further compressed, pre-purified air stream in a main heat exchanger to produce a liquid air stream; (f) expanding the liquid air stream in a liquid turbine operatively coupled to the supplemental booster compressor to produce an expanded air stream at a pressure between 7 bar(a) and 12 bar(a) and wherein the work of expansion drives the supplemental booster compressor; and (g) separating the expanded air stream into one or more oxygen enriched streams and the one or more nitrogen enriched streams in a distillation column system comprising a higher pressure column and a lower pressure column linked in a heat transfer relationship via a condenser reboiler, the distillation column system configured to receive all or a portion of the expanded air stream in the higher pressure column.
- In some embodiments, the supplemental booster compressor may be a cold booster compressor configured to receive the further compressed, pre-purified air stream, preferably at a pressure of between about 40 bar(a) and 50 bar(a) that has been partially cooled in the main heat exchanger and produce a still further compressed, pre-purified air stream at a pressure of preferably between about 50 bar(a) and 60 bar(a). Alternatively, the supplemental booster compressor may be a warm booster compressor configured to further compress the further compressed, pre-purified air stream, preferably at a pressure of between about 70 bar(a) and 90 bar(a) and before any cooling in the main heat exchanger. The warm supplemental booster compressor then produces a still further compressed, pre-purified air stream at a pressure of preferably between about 75 bar(a) and 95 bar(a).
- The portion of the compressed, pre-purified air stream received by the primary booster compressor in the present air separation unit and associated methods is preferably a boiler air stream comprising between about 25% to 45% by volume of the incoming compressed, pre-purified air stream. In some embodiments, the expanded air stream is directed to the higher pressure column of the distillation column system, whereas in other embodiments a first portion of the expanded air stream is directed to the higher pressure column of the distillation column system and a second portion of the expanded air stream is further reduced in pressure with an expansion valve and directed to the lower pressure column of the distillation column system.
- While the present invention concludes with claims distinctly pointing out the subject matter that Applicants regard as their invention, it is believed that the invention will be better understood when taken in connection with the accompanying drawings in which:
-
FIG. 1 is a schematic diagram of a cryogenic air separation unit with a conventional generator loaded liquid turbine commonly used in the prior art; -
FIG. 2 is a schematic diagram of a cryogenic air separation unit having a warm booster loaded liquid turbine in accordance with an embodiment of the present system and method for cryogenic air separation; -
FIG. 3 is an illustration of an example of a booster loaded liquid turbine used in the embodiment ofFIG. 2 ; -
FIG. 4 is a schematic diagram of a cryogenic air separation unit with a cold booster loaded liquid turbine in accordance with another embodiment of the present system and method for cryogenic air separation; and -
FIG. 5 is a graph showing data from computer simulations showing the total net compression power versus the fraction of the incoming air stream directed to the boiler air stream and comparing the prior art generated loaded liquid turbine to embodiments of a booster loaded liquid turbine. - With reference to
FIG. 1 , a prior art cryogenicair separation unit 10 employing a generator loadedliquid turbine 50 is illustrated.FIG. 2 andFIG. 4 , on the other hand, illustrate embodiments of a cryogenicair separation unit liquid turbine - As many of the components and streams in the prior art cryogenic air separation unit having a generator loaded
liquid turbine 50 are the same or similar to the present cryogenicair separation unit liquid turbines FIG. 1 ,FIG. 2 , andFIG. 4 and the reference numerals identifying the similar components are the same in each of the drawings. The differences between the prior art cryogenic air separation unit ofFIG. 1 having a generator loaded liquid turbine and the those ofFIGS. 2 and 4 having booster-loaded loaded liquid turbines, will be highlighted, as appropriate. - Cryogenic
air separation units 10. 110, 210 are each configured to receive an incomingfeed air stream 12 and produce a plurality of product streams and/or waste streams that optionally include a high pressuregaseous oxygen stream 102, a low pressuregaseous oxygen stream 104, aliquid oxygen stream 95, a liquidnitrogen product stream 90, a plurality of gaseous nitrogen enrichedstreams crude argon stream 63. Production of the streams is preferably achieved via use of a triple column fractional distillation process. In a broad sense, the depictedair separation units primary heat exchanger 60; and adistillation column system 70. - The incoming
feed air streams 12 is typically drawn through an air suction filter house (not shown) and compressed in a multi-stage, intercooled mainair compressor arrangement 20 to a pressure that can be between about 5 bar(a) and about 15 bar(a). This mainair compressor arrangement 20 may include integrally geared compressor stages or a direct drive compressor stages, arranged in series or in parallel. Thecompressed air stream 14 exiting the respective mainair compressor arrangement 20 is fed to an aftercooler with or without integral demister to remove the free moisture in the incoming feed air stream. The cool,compressed air feed 14 is then purified in apre-purification unit 25 to remove high boiling contaminants from the cool, compressed air feed. Thepre-purification unit 25, as is well known in the art, typically contains two beds or more of alumina and/or molecular sieve operating in accordance with a temperature and/or pressure swing adsorption cycle in which moisture and other impurities, such as carbon dioxide, water vapor and hydrocarbons, are adsorbed. While one of the beds is used for pre-purification of the cool, dry compressed air feed while the other bed is regenerated, preferably with a portion of the waste nitrogen from the air separation unit. The two beds switch service periodically. Particulates are subsequently removed from the compressed, pre-purified feed air in a dust filter disposed downstream of thepre-purification unit 25 to produce the compressed, purifiedair streams 28. - The compressed and purified
air stream 28 is separated into oxygen-rich, nitrogen-rich, and argon-rich fractions in a plurality of distillation columns including ahigher pressure column 72; alower pressure column 74; and an argon column arrangement, which may include anargon column 76. Prior to such distillation however, the compressed andpre-purified air streams 28 is typically split into a plurality of feed air streams, which includes at least aboiler air stream 42 and aturbine air stream 32. - The
boiler air stream 42 comprises generally between about 25% to 45% of the compressed and purifiedfeed air stream 28. Theboiler air streams 42 may be further compressed in abooster compressor arrangement 44 to a targeted pressure between about 25 bar(a) and about 90 bar(a) and subsequently cooled in aftercooler (not shown) to form a boostedpressure air stream 45. The target pressure of the boostedpressure air streams 45 is generally dictated by the product requirements for the high pressure gaseousoxygen product stream 102. The boostedpressure air stream 45 is then further cooled to temperatures required for rectification in themain heat exchanger 60 where it is used to boilliquid oxygen streams 97 via indirect heat exchange to produce the high pressure gaseousoxygen product stream 102 and/or a low pressure gaseousoxygen product stream 104. The cooled and further compressedboiler air streams 46 exitingmain heat exchanger 60 is often a liquid air stream or other dense phase fluid which is expanded in liquid turbine 50 (SeeFIG. 1 ) operatively coupled to agenerator system 52. In the embodiment shown inFIG. 2 the liquid air stream or other dense phase fluid which is expanded inliquid turbine 150 is coupled to awarm booster compressor 121 while in the embodiment shown inFIG. 4 the liquid air stream or other dense phase fluid which is expanded inliquid turbine 150 is coupled to acold booster compressor 221. - Ultimately, the expanded
streams 47 exiting theliquid turbines higher pressure column 72 and thelower pressure column 74 of thedistillation column system 70. In the illustrated embodiment, the portion of the expandedstream 47 directed to thelower pressure column 74 may be further reduced in pressure viaexpansion valve 48 yielding a lowpressure air stream 49 for introduction into thelower pressure column 74. - The
turbine air stream 32 is generally about 55% to 75% of the compressed and purifiedfeed air stream 28 and is optionally further compressed in one or moreturbine air compressors 33, cooled in an aftercooler and then directed asstream 34 to themain heat exchanger 60 where it is partially cooled prior to being directed to a turbine based refrigeration circuit that includes aturboexpander 36 as described below. The target pressure of the further compressedturbine air stream 35 is preferably between about 20 bar(a) and about 60 bar(a). The partially cooledfeed air stream 35 is expanded inturboexpander 36 to anexhaust stream 38 that is directed to thehigher pressure column 72 orlower pressure column 74 of thedistillation column system 70. In the illustrated embodiment, theexhaust stream 38 is shown directed to thehigher pressure column 72. - In some embodiments of the present system, liquid production in the cryogenic air separation units, including a pressurized liquid oxygen product stream and a liquid nitrogen product stream, may be further varied by varying the pressure in the turbine air stream sent to the turboexpander. This variation in pressure can be effectuated by a turbine air stream bypass circuit (not shown) which includes a bypass line having a bypass valve that can be set in an open or closed position. In such embodiments, the bypass circuit is configured to direct all or a portion of the turbine air stream to bypass at least one of the one or more turbine air compressors. If a bypass circuit is employed, the target pressure of the bypassed turbine air stream is preferably between about 10 bar(a) and about 30 bar(a). Also, in some embodiments that utilize the bypass circuit, it may be advantageous to provide a source of make-up nitrogen that is directed to the turbine air stream compressors in lieu of the turbine air stream so as to not damage the turbine air compressor.
- The main or
primary heat exchanger 60 is preferably a brazed aluminum plate-fin type heat exchanger. Such heat exchangers are advantageous due to their compact design, high heat transfer rates and their ability to process multiple streams. They are manufactured as fully brazed and welded pressure vessels. For small air separation unit units, a heat exchanger comprising a single core may be sufficient. For larger air separation unit units handling higher air flows, the main heat exchanger may be constructed from several heat exchange cores which may be divided into high pressure cores and low pressure cores. - The components of the feed air stream, namely oxygen, nitrogen, and argon are separated within the
distillation column system 70 that preferably includes a plurality of distillation columns in which vapor and liquid are counter-currently contacted in order to produce a gas/liquid mass-transfer based separation of the respective feed streams. Such columns will preferably employ structured packing or trays as the mass transfer contacting elements. The illustrateddistillation column system 70 includes: ahigher pressure column 72 typically configured to operate in the range from between about 20 bar(a) to about 60 bar(a); alower pressure column 74 typically configured to operate in the range from between about 1.1 bar(a) to about 1.5 bar(a); a main condenser-reboiler 75; and an argon column arrangement. The illustrated argon column arrangement preferably is configured as an argon superstaged or ultrasuperstaged column 76 with anargon condenser 77 disposed in aseparate shell 78. - The
higher pressure column 72 and thelower pressure column 74 are preferably inked in a heat transfer relationship such that a portion of the nitrogen-rich vapor column overhead, extracted from proximate the top ofhigher pressure columns 72 as astream 88 is condensed within the condenser-reboiler 75 typically located in the base oflower pressure column 74 against boiling an oxygen-richliquid column bottoms 92. The boiling of oxygen-richliquid column bottoms 92 initiates the formation of an ascending vapor phase withinlower pressure columns 74. The condensation produces a liquid nitrogenrich stream 86 that may be divided into areflux stream 87 that refluxes one or more of the distillation columns to initiate the formation of the descending liquid phase and ashelf nitrogen stream 89 that may be subcooled inheat exchanger 55 and taken as a liquidnitrogen product stream 90. Also, another portion of the nitrogen-rich vapor column overhead from thehigher pressure column 72 may be taken and warmed in themain heat exchanger 60 to produce a high pressuregaseous nitrogen stream 101. - As indicated above, a portion of the expanded
air stream 47 exiting the liquid turbine is introduced into thehigher pressure column 72 for distillation by contacting an ascending vapor phase of such mixture within a plurality of mass transfer contacting elements which may comprise trays or structured packing, with a descending liquid phase that is initiated by the reflux streams. This distillation process produces crude liquidoxygen column bottoms 82 also known as kettle liquid, and a high pressure nitrogen-rich column overhead. Similarly, a portion of the expandedair stream 47 exiting the liquid turbine is further reduced in pressure by theexpansion valve 148 and introduced into thelower pressure column 74 for distillation. The separation occurring withinlower pressure column 74 produces a nitrogen-rich vapor column overhead that is extracted as a lowpressure nitrogen stream 58 and a low pressurenitrogen waste stream 56. The separation further yields an oxygen-richliquid column bottoms 92, a portion of which may be extracted from thelower pressure column 74 as an oxygen-richliquid stream 94. - As shown in the drawings, a portion of the oxygen-rich
liquid stream 94 may be pumped viapump 96 to yield a pumpedliquid oxygen stream 97 which is directed to the associatedmain heat exchanger 60. A first portion of the pumpedliquid oxygen stream 97 is warmed to produce a high pressure gaseousoxygen product stream 102, while a second portion is reduced in pressure viavalve 98 and the resulting lowerpressure oxygen stream 99 is then warmed inmain heat exchanger 60 to produce a low pressureoxygen product stream 104. Another portion of the oxygen-richliquid stream 94 taken from thelower pressure column 74 may be taken as a liquidoxygen product stream 95. Additionally, nitrogen waste streams 106 may also be extracted fromlower pressure column 74 to control the purity of the low pressure nitrogen product streams 108. - The low pressure
nitrogen product stream 58 and thenitrogen waste stream 56 are preferably passed through one ormore subcooling units 55 designed to subcool: (i) the liquidnitrogen product stream 89; and (ii) the respective kettle streams 186,286 used to reflux theargon column 76. - The argon column arrangement is configured to receive an oxygen-
rich stream 62 typically having a concentration of about 8% to 15% by volume argon from an intermediate location of thelower pressure column 74 and separate argon and oxygen using the oxygen-rich stream 62 as an ascending vapor stream against a downflowing argon-rich reflux stream 67 received from anargon condenser 77. The mass transfer contacting elements within the argon column arrangement could be trays or structured packing. - The resulting argon-rich vapor
overhead stream 65 from theargon column 76 is then preferably directed to theargon condenser 77 where the argon-rich vapor overhead stream is condensed into a crudeliquid argon stream 66. A first portion of the crudeliquid argon stream 66 is used as the argon-rich reflux stream 67 and the remaining portion of thecrude liquid argon 66 taken as acrude argon stream 63. The oxygen rich column bottoms stream 64 from theargon column 76 is preferably returned to the lower pressure column. The cooling duty of theargon condenser 77 is provided via asubcooled stream 85 of the oxygen-enrichedstream 84 taken from thekettle liquid 82 of thehigher pressure column 72. The vaporizedportion 68 of the condensing media as well as a portion of the excess liquid in the bottom of theshell 78 may be returned to thelower pressure column 74 asstream 69. Theargon condenser 77 may be configured as a conventional argon condenser or as a down-flowing once-through argon condenser and is preferably disposed in aseparate shell 78 or alternatively disposed within thelower pressure column 74. - Turning now to
FIG. 2 , the differences between the illustrated warm booster loaded liquid turbine and the prior art generator-loaded liquid turbine ofFIG. 1 include: a booster loadedliquid turbine 150; a warm booster bypass circuit; and a liquid turbine bypass circuit. Details of the warm booster loaded liquid turbine (i.e.liquid turbine 150 that is operatively coupled to a discrete warm booster compressor 121) is discussed below and with reference to the discussion ofFIG. 3 . - The warm booster bypass circuit comprises an air circuit that includes a
diversion valve 123 configured to allow the further compressedboiler air stream 122 to bypass thewarm booster compressor 121 and send the further compressedboiler air stream 122 directly to themain heat exchanger 60 during air separation unit start-up operation and other operating conditions where the liquid turbine is off-line. In situations where thediversion valve 123 is closed, the further compressedboiler air stream 122 will be still further compressed in warm booster compressor circuit that includes thewarm booster compressor 121 and arecirculation valve 124 as well as thecontrol valve 126. - When
diversion valve 123 is closed, the further compressedboiler air stream 122 is directed to thewarm booster compressor 121. After additional compression in thewarm booster compressor 121, the still further compressedboiler air stream 128 is recirculated back upstream of thewarm booster compressor 121 via an open recirculation valve 124 (withcontrol valve 126 in ‘closed’ position) or the still further compressedboiler air stream 128 is directed to themain heat exchanger 60 via the open control valve 126 (with therecirculation valve 124 in ‘closed’ position). When thecontrol valve 126 is ‘open’ then recirculationvalve 124 anddiversion valve 123 are ‘closed’. Conversely, when thediversion valve 123 is ‘open’ then recirculationvalve 124 andcontrol valve 126 are ‘closed’. - The liquid turbine bypass circuit includes
bypass valve 153 that directs cooled compressed,boiler air stream 146 to thehigher pressure column 72 while bypassing the liquid turbine circuit. The liquid turbine circuit preferably comprisesvalve 151,liquid turbine 150, andvalve 152 which directs the resulting expandedair stream 154 to thehigher pressure column 72. Theliquid turbine 150 is generally bypassed concurrently with bypassing thewarm booster compressor 121. When bypassing theliquid turbine 150,bypass valve 153 is set in the ‘open’ position whilevalves - By using the recovered power from the
liquid turbine 150 to drive a dedicatedwarm booster compressor 121 disposed downstream of the primaryboiler air compressor 144, the required discharge pressure of the primaryboiler air compressor 144 would be lower thereby reducing the operating costs associated with the primaryboiler air compressor 144. Alternatively, one can maintain the discharge pressure of the primaryboiler air compressor 144 at design conditions and use the dedicatedwarm booster compressor 121 driven by the liquid turbine expansion to provide a net higher pressure of theboiler air stream 145 directed to themain heat exchanger 60 which in turn allows a reduction in the air flow split to the boiler air circuit. Such net higher pressure of theboiler air stream 145 translates to improved performance of theair separation unit air separation unit incoming air flow 12 can be directed to the turbine air circuit and less of theincoming air flow 12 to the boiler air circuit. In addition, there would be a capital cost savings by avoiding the capital costs associated with the generator and associated controls, partially offset by the added costs of the booster loaded liquid turbine arrangement. - Turning now to
FIG. 3 , there is shown an embodiment of the booster loadedliquid turbine 500 that employs an advanced aerodynamic design similar to other booster loaded gas turbine chassis. As seen therein, one embodiment of the booster loadedliquid turbine 500 includes a rotor assembly 510, a plurality of active magnetic bearings 520, 530 and a plurality of seals including a seal 540 disposed between the rotor assembly 510 and theliquid turbine 150 as well as a seal 550 disposed between the rotor assembly and thewarm compressor 121. - However, the size of the liquid or
dense phase turbine 150 and the coupledcompressor 121 are relatively small such that there is an aerodynamic and speed match between the turbine and the coupled gas compressor. Specifically, the pressure ratio across the dedicated warm booster compressor is preferably only about 1.1 or less, as shown in the Example ofFIG. 3 with the incoming purified, compressed air being at 1150 psia and the further compressed air stream exiting thewarm booster compressor 121 being about 1250 psia. Also, due primarily to the smaller size and lower amount of recovered power, compared to conventional booster loaded gas turbines, use of an aftercooler to cool the further compressed stream is optional and is preferably avoided to further reduce capital and operating costs. On the turbine side the incoming liquid or dense phase fluid is at 1250 psia and expanded to an exhaust stream of roughly 100 psia. The recovered work of the expansion of the fluid having liquid-like densities inturbine 150 is transferred to thewarm booster compressor 121 via rotor assembly 510. -
FIG. 4 shows a schematic diagram of a cryogenic air separation unit having a booster loadedliquid turbine 250 coupled to a cold-compressor 221. In this embodiment, the booster loaded liquid turbine is used for cold compression of all or a portion of the boiler air stream that was introduced into the main heat exchanger. In many regards the air separation unit ofFIG. 4 is similar to that of the air separation unit ofFIG. 2 except that the dedicated booster compressor is a cold compressor in lieu of the warm compressor shown inFIG. 2 . - The differences between the illustrated cold booster loaded liquid turbine in
FIG. 4 and the prior art generator-loaded liquid turbine ofFIG. 1 include: aliquid turbine 250 that is operatively coupled to acold booster compressor 221; a cold booster bypass circuit; and a liquid turbine bypass circuit. - In the embodiment of
FIG. 4 , theboiler air stream 142 in the boiler air circuit is compressed to a certain design pressure by the primaryboiler air compressor 144 and then directed to themain heat exchanger 60. The cold booster bypass circuit comprises an air circuit that includes a bypass valve 223 configured to allow the further compressedboiler air stream 145 to bypass thecold booster compressor 221 and proceed through themain heat exchanger 60 directly to thehigher pressure column 72 during air separation unit operating conditions where the liquid turbine is off-line. - In situations where the bypass valve 223 is closed, the compressed
boiler air stream 145 will be withdrawn from themain heat exchanger 60 at an intermediate location and directed to thecold booster compressor 221 viacontrol valve 226. The intermediate location of themain heat exchanger 60 generally corresponds to the location where the temperature of theboiler air stream 222 is near the boiling temperature for subcritical boiling applications. The furthercompressed stream 228 exiting thecold booster compressor 221 is then re-introduced to themain heat exchanger 60 for product boiling purposes and to thehigher pressure column 72. - The liquid turbine bypass circuit includes
bypass valve 253 that directs cooled compressed,boiler air stream 146 to thehigher pressure column 172 while bypassing the liquid turbine circuit. The liquid turbine circuit preferably comprises valve 251,liquid turbine 250, andvalve 252 which directs the resulting expandedair stream 254 to thehigher pressure column 172. Theliquid turbine 250 is generally bypassed concurrently with bypassing thecold booster compressor 221. When bypassing theliquid turbine 250,bypass valve 253 is set in the ‘open’ position whilevalves 251 and 252 are set in the ‘closed’ position. - Because the air stream is cold compressed in the embodiment of
FIG. 4 , the pressure ratio across the dedicated cold booster compressor may be higher than the pressure ratio across the dedicated warm booster compressor in the embodiment ofFIG. 2 while still maintaining the aerodynamic and speed match between the turbine and the coupled gas compressor. Using a booster loaded liquid turbine coupled to a cold compressor the pressure ratio across the cold compressor was about 1.15 enabling the air separation unit to operate with a lower inlet boiler air pressure which provides further power savings compared to the warm booster compression arrangement depicted inFIG. 2 . - Alternatively, one can maintain the discharge pressure of the primary boiler air compressor at design conditions and use the dedicated cold booster compressor driven by the liquid turbine expansion to provide a net higher pressure of the boiler air stream directed to the main heat exchanger which in turn allows a reduction in the air flow split to the boiler air circuit. Such net higher pressure of the boiler air stream translates to improved performance of the air separation unit in in the form of additional refrigeration capacity and/or power savings during operation of the air separation unit as more of the incoming air flow can be directed to the turbine air circuit and less of the incoming air flow to the boiler air circuit. In addition, there would be a capital cost savings by avoiding the capital costs associated with the generator and associated controls, partially offset by the added costs of the booster loaded liquid turbine arrangement. Specifically, computer modeling suggests that using the cold booster loaded liquid turbine arrangement of
FIG. 4 yields a power savings of about 1.8% compared to a comparably sized air separation unit without the booster loaded liquid turbine, shown generally inFIG. 1 . - The incremental capital costs realized when changing from a warm booster loaded liquid turbine arrangement to a cold booster loaded liquid turbine arrangement is manageable, but it is understood to persons skilled in the art that additional design changes to the dedicated cold booster compressor and to the main heat exchanger cores may be required.
- Using computer based simulations and models, it is projected that embodiments of the present system and method for cryogenic air separation units using a booster-loaded liquid turbine improves the cost effectiveness of air separation projects compared to installations employing a generator-loaded liquid turbine. Turning now to
FIG. 5 , there is shown a graph plotting selected results of the simulations, and particularly the expected total net compression power consumed versus the fraction of the incoming air stream directed to the boiler air stream for comparably sized cryogenic air separation units. Thefirst curve 610 on the graph represents the simulation data for a cryogenic air separation unit having a generated loaded liquid turbine with the primary boiler air compressor is configured to raise the pressure of the boiler air stream to about 1200 psia. Thesecond curve 620 on the graph represents the simulation data for a cryogenic air separation unit having an embodiment of a booster loaded liquid turbine wherein the primary boiler air compressor is configured to raise the pressure of the boiler air stream to only about 1100 psia and the supplemental booster compressor is configured further compress the boiler air stream to a pressure of about 1200 psia. Note the pressure of the boiler air stream exiting the primary boiler air compressor is lower than the baseline case of a cryogenic air separation unit having a generator loaded liquid turbine. Comparing thefirst curve 610 to thesecond curve 620, one would notice there is a small power penalty incurred when the booster-loaded liquid turbine is used compared to the generated-loaded liquid turbine at the same boiler air pressure. - However, there is a significant capital cost savings realized by switching to the booster-loaded liquid turbine arrangement which offsets the small power penalty. As discussed above, the construction and operation of a cryogenic air separation plant employing a conventional a generator-loaded liquid turbine arrangement has the disadvantage of incremental capital costs associated with generator-loading the turbine (e.g., the generator itself, structural support, electrical work, and valves/instrumentation required to facilitate safe generator start-up and speed control).
- The
third curve 630 on the graph ofFIG. 5 represents the simulation data for a cryogenic air separation unit having a booster loaded liquid turbine wherein the primary boiler air compressor is configured to raise the pressure of the boiler air stream to about 1200 psia—which is comparable to the pressure of the boiler air stream exiting the primary boiler air compressor in the baseline case—and the supplemental booster compressor is configured to further compress the boiler air stream to a pressure of about 1295 psia. Such an application may be used in retrofit situations of pre-existing air separation units to The beneficial effect of raising the boiler air stream pressure from 1200 psia exiting the primary boiler air compressor to 1,295 psia exiting the supplemental booster compressor (as represented by curve 630) in an upper column turbine cycle means less turbine air stream flow is required to produce the same or similar product slates while using less overall net compression power in the main air compressor (MAC). In addition, such pressure enhancement may allow the same air separation unit to realize better oxygen recovery and/or less incoming feed airflow. - The present system and method for cryogenic air separation units using a booster-loaded liquid turbine may also be used in air separation units where a generator-loaded liquid turbine arrangement is deemed economically unfavorable. The following table presents results of computer simulations comparing a cryogenic air separation project without the booster-loaded liquid turbine arrangement compared to a cryogenic air separation project with the booster-loaded liquid turbine arrangement having a cold booster compressor.
-
TABLE 1 Ref # Baseline ASU ASU ASU Parameter (See Drawings) w/o BLLT w/Cold BLLT Main Air Compression (MAC) Pressure 14/114 179.7 psia 179.7 psia Main Air Compression (MAC) Flow 14/114 7647 kcfh 7647 kcfh Boiler Air Compressor (BAC) Pressure 45/145 715.1 psia 625 psia Boiler Air Compressor (BAC) Flow 45/145 2200 kcfh 2143 kcfh Main Heat Exchanger U/A 60/160 9.913 MM 9.776 MM BTU/hr-k BTU/hr-k Gaseous Oxygen Flow 102/202 + 104/204 1445.2 kcfh 1445.2 kcfh Argon Flow 63/163 68.96 kcfh 68.99 kcfh Cold Booster Compressor Efficiency 221 (FIG. 4) N/A 79% Liquid Turbine Efficiency 250 (FIG. 4) N/A 79% Cold Booster Compressor Inlet Pressure 222 (FIG. 4) N/A 625 psia Cold Booster Compressor Inlet Temp 222 (FIG. 4) N/A 144° K Cold Booster Compressor Discharge P 228 (FIG. 4) N/A 717.5 psia Liquid Turbine Recovered Power 250 (FIG. 4) N/A 87.29 kW MAC Power 20/120 23263 kW 23263 kW BAC Power 44/144 3685 kW 3205 kW Total Compression Power N/A 26948 kW 26468 kW Power Savings (compared to Baseline) N/A 0 kW 480 kW - The results suggest a power savings of 480 kW for the basic same air separation unit but having the additional capital costs associated with the booster-loaded liquid turbine arrangement and modified main heat exchanger. Such power savings represents a favorable trade-off against the additional capital costs.
- While the present system and method for cryogenic air separation using a booster-loaded liquid turbine has been described with reference to one or more preferred embodiments, it is understood that numerous additions, changes and omissions can be made without departing from the spirit and scope of the present system and method as set forth in the appended claims.
Claims (12)
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Citations (3)
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DE102010052545A1 (en) * | 2010-11-25 | 2012-05-31 | Linde Aktiengesellschaft | Method and apparatus for recovering a gaseous product by cryogenic separation of air |
DE102011121314A1 (en) * | 2011-12-16 | 2013-06-20 | Linde Aktiengesellschaft | Method for producing gaseous oxygen product in main heat exchanger system in distillation column system, involves providing turbines, where one of turbines drives compressor, and other turbine drives generator |
US20140174123A1 (en) * | 2012-12-26 | 2014-06-26 | Jeremiah J. Rauch | Air separation method and apparatus |
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DE102010052545A1 (en) * | 2010-11-25 | 2012-05-31 | Linde Aktiengesellschaft | Method and apparatus for recovering a gaseous product by cryogenic separation of air |
DE102011121314A1 (en) * | 2011-12-16 | 2013-06-20 | Linde Aktiengesellschaft | Method for producing gaseous oxygen product in main heat exchanger system in distillation column system, involves providing turbines, where one of turbines drives compressor, and other turbine drives generator |
US20140174123A1 (en) * | 2012-12-26 | 2014-06-26 | Jeremiah J. Rauch | Air separation method and apparatus |
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