CN107131718A - Liquid and the method and air separation equipment of gaseous state oxygen-enriched air product are obtained in air separation equipment - Google Patents
Liquid and the method and air separation equipment of gaseous state oxygen-enriched air product are obtained in air separation equipment Download PDFInfo
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- CN107131718A CN107131718A CN201611273153.9A CN201611273153A CN107131718A CN 107131718 A CN107131718 A CN 107131718A CN 201611273153 A CN201611273153 A CN 201611273153A CN 107131718 A CN107131718 A CN 107131718A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—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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- 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
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
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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
- 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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- F25J3/04151—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
- F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
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- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
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- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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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
- F25J3/0446—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 heat generated by mixing two different phases
- F25J3/04466—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 heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid oxygen
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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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- F25J3/04763—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
- F25J3/04787—Heat exchange, e.g. main heat exchange line; Subcooler, external reboiler-condenser
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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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04793—Rectification, e.g. columns; Reboiler-condenser
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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
- 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
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- 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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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
- F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, 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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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
- F25J2200/94—Details relating to the withdrawal point
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
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- 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
- F25J2215/52—Oxygen production with multiple purity O2
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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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Oxygen, Ozone, And Oxides In General (AREA)
Abstract
The method that the application suggested low temperature air separating, wherein using with main heat exchanger (3) and distillation column system (6,7) air separation equipment (100), the distillation column system is included in the high-pressure tower (61) of first pressure level run, lower pressure column (62) and mixing column (7) in lower second pressure level run.The invention further relates to corresponding air separation equipment (100).
Description
Technical field
The present invention relates to the method for obtaining liquid and gaseous rich oxygen containing air products in air separation equipment
And it is designed to carry out the air separation equipment of such method.
Background technology
By in air separation equipment low temperature air separating produce liquid or gaseous air products be it is known, for example
In H.-W.(Hrsg.), especially in Industrial Gases Processing, Wiley-VCH, 2006
2.2.5 section " Cryogenic Rectification (cryogenic rectification) " is described.
For a series of commercial Application, pure oxygen is not needed individually at least.This is opened gives birth to air separation equipment at it
The possibility optimized in terms of production and operating cost especially its energy consumption.Referring specifically to technical literature, such as F.G.Kerry,
Industrial Gas Handbook：Gas Separation and Purification, CRC Press, the 2006, the 3.8th
Section, " Development of Low Oxygen-Purity Processes (development of hypoxemia purity technique) ".
In order to obtain the gaseous compressed oxygen compared with low-purity, particularly the air with so-called mixing column can be used to separate
Equipment, it is known already, and (corresponds to US 4,022,030 in a series of publications such as A1 of DE 2 204 376
A)US 5,454,227 A、US 5,490,391A、DE 198 03 437 A1、DE 199 51 521 A1、EP 1 139 046
B1(US 2001/052244 A1)、EP 1 284 404 A1(US 6,662,595 B2)、DE 102 09 421 A1、DE
102 17 093 1 376 037 B1 (US 6,776,004B2) of A1, EP, the A1 of EP 1 387 136 and EP 1 666 824
It is described in A1.The A1 of FR 2 895 068 also disclose that the air separation equipment with mixing column.
The liquid of oxygen be will be enriched near tower top and by the so-called mixing column air of gaseous compressed air near bottom of towe
Send into mixing column, and encounter one another.By strong contact, turn a part of volatile nitrogen from mixing column air
Move on in rich oxygen containing liquid.Rich oxygen containing liquid is evaporated at this in mixing column, and institute can be used as at the tower top of mixing column
" impure " oxygen discharge of meaning.Gas products can be used as from air separation equipment discharge unpure oxygen.Mixing column air is with regard to itself
Speech is liquefied when by mixing column, and oxygen coalescence is made to a certain extent, can be discharged from the bottom of towe of mixing column.It will can then be somebody's turn to do
Liquefied stream is on energy and/or isolation technics in suitable position feeding distillation column system used.By using mixing column,
Can be in the energy needed for feed separation is reduced in the case of considering the cost of purity of gaseous oxygen product.
The air separation equipment worked for known air separation equipment and using mixing column is disadvantageously in operation
Limited flexibility.It is general by making air in so-called blow into turbine (Einblaseturbine) in this kind equipment
Decompression, so as to cover refrigeration requirement.Such turbine that blows into makes the stress level of air from such as 5.0 to 6.0 bars be decompressed to example
Stress level such as 1.2 to 1.6 bars (is absolute pressure；Specific pressure used in scope of the invention is given below
Level).The distillation column system with (at least one) high-pressure tower and lower pressure column is provided with corresponding equipment.High-pressure tower is in institute
State the stress level under sample situation in 5.0 to 6.0 bars to run, lower pressure column is transported in the stress level of 1.2 to 1.6 bars
OK.By in the air feeding lower pressure column depressurized in blowing into turbine.Can be by given between high-pressure tower and lower pressure column
Pressure differential depressurized.But the air that decompression enters in lower pressure column in this way can disturb rectifying, thus it is generally serious
Ground limits the amount of the air depressurized in turbine is blown into and thus limit the refrigerating efficiency of the equipment.Therefore can not be from
Equipment with such connecting portion discharges the liquid form product of considerable amount.
Therefore in the legacy equipment with mixing column, the sky as being typically used for offer gaseous air product at other
The maximum of the situation of gas separation equipment (so-called gas apparatus), discharge liquid nitrogen and liquid oxygen is limited to air capacity used
A maximum of about of 0.5%.
As although the method described in the A2 of WO 2014/037091 allows to improve liquid production, but it is in order at described later
Reason, in the case of to the demand fluctuation of liquid and gaseous rich oxygen containing air products, not always provides enough spirits
Activity.
Therefore exist in the air separation equipment with corresponding mixing column efficiently and neatly production liquid it is gentle
The demand that the feasible program of the rich oxygen containing air products of state is improved.
The content of the invention
Under such background, it is proposed that being used for acquisition liquid and gaseous state in air separation equipment according to the present invention
Rich oxygen containing air products method and be set for implementing the air separation equipment of such method.Describe below preferred
Embodiment.
Turbo-compressor compressed air is used in air separation equipment.This for example suitable for " main air compressor ", its
It is characterised by, the air capacity in all feeding distillation column systems, i.e., all feeding airs is compressed by the main air compressor.
Correspondingly, " later stage compressor " can also be set, wherein a part for the air capacity compressed in main air compressor is being applied
Add to higher pressure.It can also be configured to turbo-compressor.For compression section air capacity, other whirlpools are typically set
Wheel compression machine, the turbo-compressor is also referred to as supercharger, but relative to main air compressor or later stage compressor only to compare
Small degree is compressed.
In addition multiple positions that can be in air separation equipment depressurize air, and letter herein can be used by being particularly for this
The referred to as negative booster of the form of the turbine expander of " turbine ".Turbine expander can also be connected and drive with turbo-compressor
Move the turbo-compressor.If one or more turbo-compressor in the case of no outside input energy i.e. only by one or
Multiple turbine expanders drive, then also use term " turbocharger " for such arrangement.In turbocharger,
Turbine expander is mechanically connected with turbo-compressor.
The application characterizes pressure and temperature using term " stress level " and " temperature levels ", thus expresses corresponding
Pressure and temperature need not be used in the form of accurate pressure value or temperature value in equipment, to realize the solution of the present invention.But
Such pressure and temperature generally in certain scope fluctuate, for example around intermediate value fluctuation ± 1%, 5%, 10%, 20% or
Even 50%.In general, the numerical value in one " level " is more or less the same in 5% or 10% each other.Here, corresponding pressure
Level and temperature levels can be in discontinuous scope or in overlapped scopes.For example stress level is especially wrapped
The inevitable pressure loss or the expected pressure loss are included, it is for example because cooling effect or transmission loss cause.Accordingly
It is also applied for temperature levels.The stress level provided herein with bar is related to absolute pressure.
What is discussed in the category of the application is to obtain air products, air products especially rich in oxygen and rich in nitrogen or
Oxygen product and nitrogen product." product " leaves the equipment and stores or consume for example in tank.Therefore it is no longer only independent
The circulation of device interior is participated in, but can correspondingly be used before the equipment is left, for example, is made in a heat exchanger
For cold carrier.Therefore, term " product " is not including itself staying in the device and individually being used for example as flowing back herein, cool down
Agent or the cut or stream of purge gas.
In addition, term " product " includes given amount." product " is corresponding to the air capacity used in corresponding equipment
At least 1%, especially at least 2%, for example, at least 5% or at least 10%.Therefore, it is less amount of generally also in the gas apparatus
The middle liquid fraction for producing and optionally being discharged by the equipment is not " product " in the sense that the application.For example in known distillation
In Tower System, a small amount of liquid fraction separated in bottom of towe is discharged from lower pressure column all the time, to avoid unexpected component such as methane
Enrichment.But its due to the amount so not being " product " in the sense that the application.By discharging liquid form product, from air point
From equipment " discharge " considerable cold, these colds additionally can be reclaimed partly by the evaporation of this liquid form product.But
It is that such discharge is only just worked from specific discharge rate, i.e., actually discharges " product " in meaning defined above
In the case of.
Liquid or gaseous " rich oxygen containing air products " are corresponding state of aggregations in the language usage of the application
Fluid, the fluid has the oxygen content based on mole, at least the 75% of weight or volume, especially at least 80%.Therefore, from
" unpure oxygen " of mixing column discharge is also rich oxygen containing air products.
Invention advantage
It is proposed that the method for low temperature air separating, wherein using the air with main heat exchanger and distillation column system
Separation equipment, the distillation column system is included in the high-pressure tower of first pressure level run, the low pressure in second pressure level run
Tower and mixing column.Second pressure level is less than first pressure level.
For example as disclosed in the foregoing A2 of WO 2014/037091, can in such method, from the lower pressure column with
Rich oxygen containing stream of the liquid discharge with the first oxygen content, the stream is not separated directly with liquid or the state of evaporation from the air
Equipment is exported, but is especially sent into after the heating with the first oxygen content with liquid in the mixing column, especially sends into top
In region, such as in tower top.In addition the first compressed air stream is sent into the mixing column with gaseous state, and in the mixing column
Send to and meet the rich oxygen containing stream with the first oxygen content.Mixed it is preferred that directly sending into the first compressed air stream above bottom of towe
In tower.
By so running the mixing column, it can be discharged from the mixing column in tower top side with less than the first oxygen content
The rich oxygen containing stream of second oxygen content, and exported as gaseous rich oxygen containing air products from the air separation equipment.
Rich oxygen containing stream with the second oxygen content is " impure " oxygen, but its (second) oxygen content is for specific purposes
Enough, and the optimization on described energy can be realized.
In corresponding equipment, pure oxygen stream can be discharged with liquid from lower pressure column especially its bottom of towe and be made with its oxygen content
Exported for the rich oxygen containing air products of liquid with liquid from the air separation equipment.Correspondingly in WO 2014/037091
Shown in A2.The pure oxygen stream has the oxygen content higher than the first oxygen content.Therefore provide another with height in the case
The rich oxygen containing air products of the liquid of oxygen content.Thus what is carried out (has from the oxygen containing stream of two bursts of richnesses of lower pressure column discharge
Have the rich oxygen containing stream and extra pure oxygen stream of the first oxygen content) it is alternative in technology, condition is except gaseous state
Rich oxygen containing air products beyond also need to pure liquid oxygen form liquid rich oxygen containing air products.If not needing such pure
The rich oxygen containing air products of the liquid of liquid oxygen form, or the required purity of the rich oxygen containing air products of liquid compare gaseous state
Rich oxygen containing air products desired purity it is high about 1 to 2 percentage point, then can also be from the lower pressure column only with liquid
The rich oxygen containing stream of discharge.Then a portion can be for example sent into mixing column as previously described, and by a part with liquid
Form is exported from the air separation equipment, i.e., the rich oxygen containing air products as liquid.
In all cases, liquid is temporarily, at least also exported with liquid from the air separation equipment in the present invention
Rich oxygen containing air products, such as rich oxygen containing air products of the corresponding liquid from lower pressure column with the first oxygen content
Or corresponding pure oxygen.Other rich oxygen containing air products can also be exported from the air separation equipment with liquid.As product,
Its amount at least includes above for " product " given value.Corresponding liquid can be exported from the air separation equipment with liquid
The amount of the rich oxygen containing air products of state is due to being very flexible according to measure as suggested in the present invention.
If previously discussed is rich oxygen containing stream, i.e., especially there is the rich oxygen containing stream of the first oxygen content and be optionally present
Pure oxygen stream with higher oxygen content and other rich oxygen containing streams discharged from the lower pressure column with liquid, then herein relate to
Stream for producing corresponding rich oxygen containing air products.Therefore, as described above for term " product " Suo Shu, these streams are not with substantially
The stream for being same as providing not as product is for example only used for for example going the amount of deimpurity flush out stream from institute from the bottom of towe of lower pressure column
State lower pressure column export.Therefore the rich oxygen containing pure oxygen stream for flowing and being optionally present and others with the first oxygen content are rich oxygen containing
Flow respectively to discharge from the lower pressure column above for the amount in the scope described in " product ".
In scope of the invention, the first compressed air stream in feeding mixing column is by using being compressed into higher than the
The initial pressure level of one stress level and then the first temperature levels are especially cooled in the main heat exchanger and
The air formation depressurized in one turbine.As described below, especially this is used in so-called HAP methods (" high air pressure ")
The whole air capacities for delivering to distillation column system, i.e., be wherein compressed to apparently higher than the highest used in distillation column system by invention
The method of the pressure of operating pressure.Here, " apparently higher than " is interpreted as at least 1.0 bars, especially bigger pressure in the case
Power is poor.By using corresponding first turbine, extra cold can be produced, cold compensation is particularly due to from air point
From loss of refrigeration capacity caused by the rich oxygen containing air products that equipment discharges liquid.In scope of the invention, used by depressurizing
A part of refrigeration requirement is covered in the air for providing the first compressed air stream, the air is depressurized in first turbine.
In addition, the present invention also advises, the second compressed air stream is sent into the high-pressure tower, second compressed air stream is same
Sample be by using be compressed into initial pressure level then be especially cooled in main heat exchanger the first temperature levels and
The air formation depressurized in the first turbine.Therefore, a part for the air depressurized in the first turbine is at it
After being depressurized in one turbine in feeding mixing column, in another part feeding high-pressure tower.
In addition, the present invention also advises, the 3rd compressed air stream is sent into the lower pressure column, the 3rd compressed air stream is
By using be compressed into initial pressure level then be especially cooled in the main heat exchanger second temperature level,
Then decompression is cooled further to the air formation of the 3rd temperature levels in the main heat exchanger in the second turbine.
In scope of the invention, air is decompressed to first pressure level, i.e. high-pressure tower in first turbine
Stress level, and it is decompressed in the second turbine the stress level of second pressure level, i.e. lower pressure column.The mixing column is at this
It is the stress level of high-pressure tower in the first pressure level in the category of invention or is differing most 1 with first pressure level
The 3rd stress level operation of bar.
The air depressurized in the first turbine and the air that is depressurized in the second turbine in scope of the invention
First temperature levels send into the first turbine and send into the second turbine in second temperature level, wherein the first temperature levels compare the
Two temperature levels low at least 20K, especially at least 30K or at least 40K.First temperature levels can especially compare second temperature
Level low 25 to 35K or 28 to 32K, particularly from about 30K.For each temperature levels, also referring to following explanation.Here, first
Turbine is " cold " turbine, and the second turbine is " hot " turbine.
If expecting to subtract in the HAP methods of aforementioned type and traditional method or equipment using mixing column is wherein realized
Few liquid production, i.e., exported the amount of the air products of liquid with liquid from air separation equipment, then must flow through main sky
The pressure of main air compressor is reduced in the case of the constant amount of air of air compressor.But in the case of constant amount of air phase
The pressure that answering ground reduces increases the actual volume of the air of compression.Therefore, in traditional equipment, it is arranged in the dress of hot part
The size for putting especially air purge and precooling unit must be significantly larger.This is to be unworthy expecting for economic reasons
's.In addition, reducing pressure in the case of constant amount of air, this is not usually in terms of effect of main air compressor used
Optimal.
High pressure pressure tower is clearly lower or higher than for the mixing pressure tower for wherein depending on pressure needed for gaseous oxygen product
Method there is provided the method described in the foregoing A2 of WO 2014/037091.
Unlike this, according to present invention recognizes that, if pressure needed for pressure product is at or approximately at the high pressure of about 5 bars
Pressure tower level is first pressure level or the 3rd stress level of most 1 bars is differed with first pressure level, such as in the present invention
Category in, then in the case that HAP methods press turbine and blow into turbine (Einblaseturbine) in use provide liquid
It is favourable in terms of the equipment flexibility of state oxygen product and operating cost.
" middle-pressure turbine " is the first described turbine, and " blowing into turbine " is by second in the category of the application
Turbine formation.Because the method according to the invention is designed to HAP methods, unique main air compressor is only needed,
This significantly reduces cost of investment.The inlet pressure of the two turbines is preferably in identical level, is particularly in main sky
The level of the outlet pressure of air compressor.
, can in scope of the invention if comparatively large number of liquid oxygen product (" higher liquid production ") should be provided
To raise initial pressure level (stress level provided by main air compressor), while increasing empty with the 3rd compression for this
(decompression " blows into sky to the amount of air in the form feeding lower pressure column of air-flow i.e. in the second turbine is " blowing into turbine "
Gas ").Therefore, because increasing the amount of the air depressurized in the second turbine, improve so-called " air factor ", i.e., it is total
It is common to the air capacity needed for rectifying.
By it is described while rise pressure and amount so that the equipment produces bigger efficiency, and main air compressor is defeated
Go out bigger efficiency, and liquid production can be increased.Make the actual volume of the air in hot part simultaneously in the model of the present invention
Approximately constant is kept in farmland, because improving pressure and amount.In the performance plot of main air compressor, improve in this way
The amount and pressure of the air of compression, this typically advantageously influences effect of main air compressor.
Unlike this, if more a small amount of liquid oxygen product (" relatively low liquid production ") should be provided, reduction is initial
Stress level, while reducing the amount of the air to be sent into the form of the 3rd compressed air stream in lower pressure column for this.Due to reducing
The amount of the air depressurized in the second turbine, reduces air factor.
By reducing pressure and decrement simultaneously so that the equipment produces less efficiency, main air compressor output
Smaller power, and reduce liquid production.The actual volume of the air in hot part is set to keep approximately constant again simultaneously.
In the performance plot of main air compressor, the amount and pressure of the air of compression are reduced in this way, this and simple reduction pressure phase
Than typically advantageously influenceing effect of main air compressor.
In scope of the invention, advantageously using the 4th compressed air stream in feeding high-pressure tower, the 4th compression is empty
Air-flow is by using the sky for being compressed into initial pressure level, being subsequently cooled to the 3rd temperature levels and being depressurized by flow controller
Gas formation.Corresponding 4th compressed air stream corresponds to the throttling stream of traditional air separating method.
The method according to the invention advantageously comprises the first technology pattern and the second technology pattern, wherein in the first technique mould
The rich oxygen containing air for exporting liquid with the amount bigger relative to the second technology pattern with liquid from air separation equipment in formula is produced
Product, wherein the air capacity bigger relative to the second technology pattern is depressurized in the second turbine in the first technology pattern, and by
This is while the 3rd compressed air stream includes the same air capacity bigger relative to the second technology pattern in the first technology pattern.Change
For it, in order to discharge the rich oxygen containing air products of a greater amount of liquid in scope of the invention, improve and pass through the second whirlpool
Turbine, which is depressurized and sent into lower pressure column, blows into air capacity.It is possible thereby to cover extra due to what is discharged liquid oxygen product and produce
Refrigeration requirement.
Rich oxygen containing air products respectively since liquid derived from air separation equipment are discharged from lower pressure column.Herein can be with
Using pure oxygen, as described above, or liquid oxygen product of the use with lower oxygen content.If " being exported with liquid " this fluid-like state
Rich oxygen containing air products, then it means that in air separation equipment without evaporation.If given above in the first technique
Export the rich oxygen containing air of liquid in pattern with liquid with the amount bigger relative to the second technology pattern from air separation equipment
Product, then this can also include, do not export the rich oxygen containing air products of liquid in the second technology pattern.In the first technique mould
With liquid, the amount of the rich oxygen containing air products of liquid can for example be included in the second work derived from air separation equipment in formula
1.5 times, 2 times, 3 times, 4 times or 5 times of corresponding amount in skill pattern.
Consider it is so-called blow into equivalent in the case of advantageously increase in the second turbine decompression simultaneously by the 3rd
The air capacity that compressed air stream includes.This blows into equivalent includes the amount of the air capacity by the second turbine pressure relief, the amount first
Simultaneously corresponding to the air capacity included by the 3rd compressed air stream；It is also extra to include the same stream rich in nitrogen discharged from high-pressure tower
Amount.These streams rich in nitrogen are liquid nitrogen and compressed nitrogen, are used as the air products rich in nitrogen of corresponding air separation equipment
Supply.These streams rich in nitrogen, which are not used as liquid reflux, is used for high-pressure tower and lower pressure column.More advantageously, in the second turbine
The air capacity and the summation of the amount of the stream rich in nitrogen that middle decompression is included by the 3rd compressed air stream simultaneously are in the first technique mould
Formula includes 12 to 18% of the total air in all feeding distillation column systems, includes total air in the second technology pattern
0 to 8%.Total air in all feedings distillation column system is additionally included in the air depressurized in the second turbine.
A kind of such change programme especially realizes as follows, the first turbine constructed in the way of variable speed or
Operation, so as to realize correspondingly different air throughputs in different operational modes.In the category of the application, art
Language " variable speed " turbine is solely for for example being set as fixing by the brake correspondingly adjusted relative to its rotating speed
The boundary of the turbine of tachometer value.Corresponding situation is also applied for the second turbine.
As described, the method according to the invention is advantageously combined so-called HAP methods and used, wherein by using primary air pressure
Air in all feeding distillation column systems is compressed to the stress level higher than high-pressure tower stress level by contracting machine.Therefore it is favourable
It is to be applied the air in all feeding distillation column systems to initial pressure level by using main air compressor.
In scope of the invention, as described in other words, air factor is used to be consolidated in the first technology pattern
The air capacity of fixed product volume is significantly greater than the second technology pattern, because decompression is simultaneously by the 3rd pressure in the second turbine
Air capacity in stream of compressed air includes, feeding lower pressure column is more than the second technology pattern.In the first technology pattern, as described,
The discharge liquid form product amount bigger relative to the second technology pattern.Therefore it must also guide bigger relative to the second technology pattern
Air capacity passes through main air compressor.But, herein due to bigger air factor, the final pressure of main air compressor exists
This stress level for being referred to as " initial pressure level " is consistently less than the less situation of air factor.
Unlike this, air factor is significantly less than the first technology pattern in the second technology pattern, because second
The air capacity depressurized in turbine in included by the 3rd compressed air stream, feeding lower pressure column simultaneously is less than the first technology pattern.
In the second technology pattern, as described, the discharge liquid form product amount smaller relative to the first technology pattern.This causes relative to
One technology pattern reduces air capacity of the guiding by main air compressor, while final pressure (is referred to herein as " initial pressure
The stress level of level ") it is lower.As described, unlike this, must keep guiding logical under reduced pressure in conventional methods where
The air capacity for crossing main air compressor is constant, and this causes the actual volume of the air capacity to increase.In scope of the invention no longer
It is such situation, therefore the load condition in the second operational mode no longer determines chi for the heat part of air separation equipment
It is very little.While the pressure on the final pressure (i.e. " initial pressure level ") of main air compressor in the first and second technology patterns
Power difference is less than situation in conventional methods where, because as described due to bigger air factor so that in the first technique mould
The final pressure of main air compressor remains less than the less situation of air factor in formula.Because reducing in main air compressor
The air capacity of middle compression and reduce the pressure used herein, thus the load condition it is general in performance plot better than compression
The situation that constant amount of air and pressure more decline to a great extent.
Advantageously, the air depressurized in the first turbine and the second turbine is especially first in identical stress level
Beginning stress level sends into the first turbine and the second turbine.Advantageously, in scope of the invention, herein in the first technique mould
Initial pressure level in formula is than high 1 to 10 bar of initial pressure level in the second technology pattern.Generally, the application's
In category, initial pressure level may be at 6 to 15 bars, and first pressure level may be at 4.3 to 6.9 bars, especially about 5.4
Bar, second pressure level may be at 1.3 to 1.7 bars, especially about 1.4 bars.If mixing column is not in first pressure level fortune
OK, then the 3rd stress level differs most 1 bars with first pressure level as described.First temperature levels are preferably 110 to 140
DEG C, second temperature level is 130 to 240 DEG C, and the 3rd temperature levels are 97 to 102 DEG C.
The turbine used in scope of the invention can be braked in a different manner.Can especially use generator,
Supercharger and/or oil brake.
The method according to the invention is especially adapted for use in situations below, wherein the first oxygen content is 99 moles of below %, example
Such as 98 to 99 moles of %, the second oxygen content is 80 to 98 moles of %.If being formed, the oxygen content of pure oxygen stream be advantageously 99 to
100 moles of %.It is proved to be particularly effective in terms of energy in these cases using the method for mixing column.
In addition, the present invention also extends into the air separation equipment with main heat exchanger and distillation column system, the destilling tower
System includes being designed in the high-pressure tower of first pressure level run, being designed in the low pressure of lower second pressure level run
Tower and mixing column.
In corresponding equipment, the device for following purpose is provided with：There is the first oxygen with liquid discharge from lower pressure column
Content it is rich it is oxygen containing stream and with the first oxygen content with liquid feeding mixing column in, especially in upper area；In addition by
One compressed air stream in mixing column in gaseous state feeding mixing column, especially near bottom of towe, and to send to and meet with first
The rich oxygen containing stream of oxygen content；Discharged from mixing column in tower top side and be rich in oxygen with the second oxygen content for being less than the first oxygen content
Stream and from air separation equipment export；And by using be compressed into higher than first pressure level initial pressure level,
It is subsequently cooled to the first temperature levels and the air depressurized in the first turbine the first compressed air stream of formation.
As described, pure oxygen stream can also be discharged with liquid from lower pressure column and exported from air separation equipment with liquid.Herein
The device of this setting is existed in the case of class.It is at least temporary transient from air separation equipment there is provided being designed in all cases
Ground exports the device of the rich oxygen containing air products of liquid with liquid.
The device arranged according to the present invention having for following purpose, the second compressed air stream is sent into high-pressure tower, and this
Two compressed air streams are again by using being compressed into initial pressure level, be subsequently cooled to the first temperature levels and first
The air formation depressurized in turbine；3rd compressed air stream is sent into lower pressure column, the 3rd compressed air stream is to pass through
Using be compressed into initial pressure level, be subsequently cooled to second temperature level, in the second turbine decompression and it is main heat hand over
The air formation of the 3rd temperature levels is cooled further in parallel operation；Air is decompressed to first pressure water in the first turbine
Put down and second pressure level is decompressed in the second turbine；Mixing column first pressure level or with first pressure level phase
The 3rd stress level operation of most 1 bars of difference.
In addition these devices are designed to following purpose according to the present invention, the air that is depressurized in the first turbine and
The air depressurized in second turbine is to send into the first turbine in the first temperature levels and send into second in second temperature level
Turbine, wherein the first temperature levels at least 20K lower than second temperature level.
Such air separation equipment is especially designed to run in the first technology pattern and the second technology pattern, this
It is to be realized by the device being provided with for following purpose：From air separation equipment with relative in the first technology pattern
The bigger amount of two technology patterns exports the rich oxygen containing air products of liquid with liquid, and in the first technology pattern, second
The air capacity bigger relative to the second technology pattern is depressurized in turbine, so as to thus make the 3rd compressed air stream in the first technique
Pattern includes the same air capacity bigger relative to the second technology pattern.
The present invention is explained in more detail according to accompanying drawing below, which show the preferred embodiment of the present invention.
Brief description of the drawings
Fig. 1 shows the air separation equipment according to one embodiment of the invention in the form of exemplary device figure.
Embodiment
The air separation equipment according to a particularly preferred embodiment of the present invention is shown in Fig. 1, its totality
It is upper to be represented with 100.
Feed air stream a is drawn via filter 1 from air separation equipment 100 by main air compressor 2, shown
The stress level of 6 to 15 bars (absolute) is compressed in embodiment.The drying of known type can and then be implemented after being compressed
Step, cooling step and purification step, it is for the sake of clarity not shown in Fig. 1.
The air stream b for correspondingly compressing and purifying is divided into two tributaries c and d, is sent into the stress level in hot side
Main heat exchanger 3, wherein cooling is simultaneously discharged in different temperature levels.
From tributary c by being discharged from main heat exchanger 3 in different temperature levels formation two gangs of tributaries e and f.Tributary e
Depressurized in negative booster 4, tributary f is depressurized in negative booster 5.Because tributary e is cooled to relative to tributary f lower temperatures,
So negative booster 4 is also referred to as " cold " negative booster, unlike this, negative booster 5 is referred to as " hot " negative booster.
This two gangs of tributaries e and f decompression are each come into effect with the stress level of 5 to 15 bars (absolute).Tributary e exists
The stress level of about 5.4 bars (absolute) is decompressed in shown embodiment, unlike this, tributary f is decompressed to about 1.4 bars
The stress level of (absolute).Generator 41 and 51 is connected with negative booster 4 and 5 respectively.
Tributary e is again split into two gangs of tributaries g and h after it is depressurized in negative booster 4.Tributary g sends into height near bottom of towe
Tower 61 is pressed, the high-pressure tower is configured to a part for double tower 6.H decompressions near bottom of towe in tributary enter in mixing column 7.High-pressure tower 61
Run in the stress level of about 5.4 bars (absolute), lower slightly stress level operation of the mixing column 7 in about 5.0 bars (absolute).
Tributary f is sent back in main heat exchanger 3 after it is depressurized in negative booster 5 in medium temperature level, is handed over from the main heat
Parallel operation is discharged and sent into lower pressure column 62 in cold side, and the lower pressure column is likewise constructed to a part for double tower 6.Lower pressure column 62 is about
The stress level operation of 1.4 bars (absolute).
Tributary d is discharged from main heat exchanger 3 in cold side, and starts decompression with the stress level of 6 to 15 bars (absolute)
Into in high-pressure tower 61.
The rich oxygen containing cut of liquid is isolated in bottom of towe side in high-pressure tower 61, and is discharged in the form of flowing i.Guiding stream
I is by being subcooled adverse current device 8, and then decompression enters in lower pressure column 62.
Overhead product rich in nitrogen is discharged from the tower top of high-pressure tower 61, and part guiding in the form of flowing k passes through double tower 6
Main condenser 63, and liquefy at least in part herein.The overhead product rich in nitrogen of the liquid of high-pressure tower 61 a part (referring to
Connection A) in the form of flowing 1 guiding by being subcooled adverse current device, and as liquid the air products rich in nitrogen in equipment boundary
Discharge.Another part of the liquefied overhead product rich in nitrogen of high-pressure tower 61 returns to high-pressure tower 61 as backflow.
It is same to guide by the way that adverse current device 8 is subcooled, and in tower top from the stream m of the middle column plate discharge nitrogen enrichment of high-pressure tower 61
Nearby decompression enters in lower pressure column 62.
The rich oxygen containing cut of liquid is formed in the bottom of towe of lower pressure column, its (referring to connection B) is discharged in the form of flowing n,
Partly guide by the way that adverse current device 8 is subcooled, and discharged as the rich oxygen containing air products of liquid in equipment boundary.
The stream o of oxygen coalescence is discharged from the middle column plate of lower pressure column 62, by pump 9 with liquid-applied pressure, guiding passed through
Cold adverse current device 8, is heated in main heat exchanger 3 and in feeding mixing column 7 near tower top.Side of the mixing column 7 as described in repeatedly
Formula is run.Discharged from the tower top of mixing column 7 makes the stream p of oxygen dilution relative to stream o, heats and be used as gas in main heat exchanger 3
The oxygen product of state is discharged in equipment boundary.
Impure nitrogen stream q is discharged from the tower top of lower pressure column 62, is guided by the way that adverse current device 8 and main heat exchanger 3 and example is subcooled
In purification devices such as flowing a.
The stream r rich in nitrogen is formed by main condenser 63, nitrogen enrichment overhead product without guiding by lower pressure column 61.
Air separation equipment 100 shown in Fig. 1 is designed to two kinds of foregoing technology patterns.In the first technology pattern
In herein in the form of flowing n as derived from air separation equipment 100 with liquid the air products of liquid amount be more than the second technique
Pattern.The air capacity bigger relative to the second technology pattern is depressurized via turbine 5 in the first technology pattern simultaneously, so as to carry
High air factor.In the second technology pattern, due to the air factor of reduction, stream b pressure and amount, i.e. primary air pressure is reduced
The amount for the air that the final pressure of contracting machine 2 and guiding pass through the main air compressor.
Claims (15)
1. the method for low temperature air separating, wherein being separated using the air with main heat exchanger (3) and distillation column system (6,7)
Equipment (100), the distillation column system is included in the high-pressure tower (61) of first pressure level run, in lower second pressure level
The lower pressure column (62) and mixing column (7) of operation, wherein
- discharge the rich oxygen containing stream (n) with the first oxygen content and from the lower pressure column (62) with liquid with the first oxygen content
Sent into liquid in the mixing column (7),
- in addition send into the first compressed air stream (h) in the mixing column (7) with gaseous state, and sent in the mixing column (7)
The rich oxygen containing stream (n) with the first oxygen content is met,
- the rich oxygen containing stream (o) of the second oxygen content with less than the first oxygen content is discharged in tower top side simultaneously from the mixing column (7)
From the air separation equipment (100) export,
- first compressed air stream (h) is by using the initial pressure level being compressed into higher than first pressure level, so
After be cooled to the first temperature levels, send into the first turbine (4) in first temperature levels and subtract in first turbine (4)
The air formation of pressure, and
- from the air separation equipment (100) temporarily, at least with liquid export liquid rich oxygen containing air products,
Characterized in that,
- send into the second compressed air stream (g) in the high-pressure tower (61), second compressed air stream is again by using quilt
It is compressed to initial pressure level, is subsequently cooled to the first temperature levels and the air formation of decompression in the first turbine (4),
- send into the 3rd compressed air stream (f) in the lower pressure column (62), the 3rd compressed air stream is by using being compressed
To initial pressure level, it is subsequently cooled to second temperature level, in the second temperature level the second turbine of feeding (5), at this
The air for being depressurized in second turbine (5) and the 3rd temperature levels being cooled further in the main heat exchanger (3) is formed
,
- air is decompressed to first pressure level in first turbine (4) and is decompressed in second turbine (5)
Second pressure level, the mixing column (7) differs most 1 bars in the first pressure level or with the first pressure level
3rd stress level is run, and
- the first temperature levels at least 20K lower than the second temperature level.
2. method according to claim 1, wherein the 4th compressed air stream (f) is sent into the high-pressure tower (62), the 4th
Compressed air stream is by using being compressed into initial pressure level, is subsequently cooled to the 3rd temperature levels and subtracts by flow controller
The air formation of pressure.
3. according to the method for claim 1 or 2, it includes the first technology pattern and the second technology pattern, wherein
- in the first technology pattern, exported from the air separation equipment (100) with the amount bigger relative to the second technology pattern
The rich oxygen containing air products of liquid,
- in the first technology pattern, the decompression air bigger relative to the second technology pattern in second turbine (5)
Amount, and thus the 3rd compressed air stream (f) includes equally relative to the second technology pattern in the first technology pattern simultaneously
Bigger air capacity.
4. method according to claim 3, wherein discharging the one or more strands of streams (l, q) rich in nitrogen simultaneously from the high-pressure tower (61)
From the air separation equipment (100) export, wherein decompression is simultaneously empty by the described 3rd compression in second turbine (4)
The air capacity that air-flow (f) includes is adjusted as follows so that simultaneously described by second turbine (4) decompression
The amount for the air capacity that 3rd compressed air stream (f) includes and the amount that is included by the one or more strands of streams (l, q) rich in nitrogen
Summation corresponds to the 12 to 18% of the total air being admitted in the distillation column system (6,7) in the first technology pattern,
Correspond to the 0 to 8% of the total air in second technology pattern.
5. according to the method for claim 3 or 4, wherein by using main air compressor (2) by the distillation of all feedings
Air in Tower System (6,7) applies to initial pressure level.
6. method according to claim 5, wherein in the first technology pattern, by the air bigger relative to the second technology pattern
Guiding passes through the main air compressor (2) to amount at a higher pressure.
7. according to the method for one of preceding claims, wherein the sky depressurized in the first turbine (4) and the second turbine (5)
Gas is to send into the first turbine (4) and the second turbine (5) in identical stress level.
8. according to the method for one of claim 3 to 7, wherein the initial pressure level ratio in the first technology pattern is in the second work
High 1 to 10 bar of initial pressure level in skill pattern.
9. according to the method for one of preceding claims, wherein initial pressure level is in 6 to 15 bars (absolute), first pressure water
Flat to be in 4.3 to 6.9 bars (absolute), second pressure level is in 1.3 to 1.7 bars (absolute).
10. according to the method for one of preceding claims, wherein the first temperature levels are in 110 to 140 DEG C, second temperature level
In 130 to 240 DEG C, the 3rd temperature levels are in 97 to 102 DEG C.
11. according to the method for one of preceding claims, wherein first turbine (4) and/or second turbine (5)
Braked by using generator, supercharger and/or oil brake.
12. according to the method for one of preceding claims, wherein first oxygen content is 99 to 100 moles of %, described second
Oxygen content is 80 to 98 moles of %.
13. according to the method for one of preceding claims, wherein first turbine (4) and second turbine (5) are
The turbine of variable speed.
14. air separation equipment (100), it has main heat exchanger (3) and distillation column system (6,7), the distillation column system bag
Include the high-pressure tower (61) for being designed in first pressure level run, the lower pressure column for being designed in lower second pressure level run
(62) and mixing column (7), it is provided with the device for following purpose：
- discharge the rich oxygen containing stream (n) with the first oxygen content and from the lower pressure column (62) with liquid with the first oxygen content
Sent into liquid in the mixing column (7),
- in addition send into the first compressed air stream (h) in the mixing column (7) with gaseous state, and sent in the mixing column (7)
The rich oxygen containing stream (n) with the first oxygen content is met,
- the rich oxygen containing stream (o) of the second oxygen content with less than the first oxygen content is discharged in tower top side simultaneously from the mixing column (7)
From the air separation equipment (100) export,
- first compressed air stream (h) is by using the initial pressure level being compressed into higher than first pressure level, so
After be cooled to the first temperature levels, send into the first turbine (4) in first temperature levels and subtract in first turbine (4)
The air formation of pressure, and
- from the air separation equipment (100) temporarily, at least with liquid export liquid rich oxygen containing air products,
It is characterized in that the device for following purpose
- send into the second compressed air stream (g) in the high-pressure tower (62), second compressed air stream is again by using quilt
It is compressed to initial pressure level, is subsequently cooled to the first temperature levels and the air formation of decompression in the first turbine (4),
- send into the 3rd compressed air stream (f) in the lower pressure column (62), the 3rd compressed air stream is by using being compressed
To initial pressure level, it is subsequently cooled to second temperature level, in the second temperature level the second turbine of feeding (5), at this
The air for being depressurized in second turbine (4) and the 3rd temperature levels being cooled further in the main heat exchanger (3) is formed
,
- air is decompressed to first pressure level in first turbine (4) and is decompressed in second turbine (5)
Second pressure level, the mixing column (7) differs most 1 bars in the first pressure level or with the first pressure level
3rd stress level is run, and
- first temperature levels at least 20 Ks lower than the second temperature level.
15. air separation equipment (100) according to claim 14, it is designed in the first technology pattern and the second technique
Run in pattern, this is realized by the device being provided with for following purpose
- in the first technology pattern, exported from the air separation equipment (100) with the amount bigger relative to the second technology pattern
The rich oxygen containing air products of liquid,
- in the first technology pattern, the decompression air bigger relative to the second technology pattern in second turbine (5)
Amount, so that it is same relative to the second technology pattern thus to make the 3rd compressed air stream (f) include in the first technology pattern
Bigger air capacity.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP15003483.3 | 2015-12-07 | ||
| EP15003483.3A EP3179186A1 (en) | 2015-12-07 | 2015-12-07 | Method for obtaining a liquid and a gaseous oxygen-rich air product in an air breakdown apparatus and air breakdown apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107131718A true CN107131718A (en) | 2017-09-05 |
| CN107131718B CN107131718B (en) | 2020-12-22 |
Family
ID=54838147
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611273153.9A Active CN107131718B (en) | 2015-12-07 | 2016-12-06 | Method for obtaining liquid and gaseous oxygen-enriched air products in air separation plant and air separation plant |
Country Status (7)
| Country | Link |
|---|---|
| EP (2) | EP3179186A1 (en) |
| CN (1) | CN107131718B (en) |
| AU (1) | AU2016269434B2 (en) |
| BR (1) | BR102016028677B1 (en) |
| CL (1) | CL2016003150A1 (en) |
| PL (1) | PL3179187T3 (en) |
| RU (1) | RU2722074C2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112469952A (en) * | 2018-08-22 | 2021-03-09 | 林德有限责任公司 | Air separation plant, method for the cryogenic separation of air by means of an air separation plant and method for creating an air separation plant |
| WO2022016416A1 (en) * | 2020-07-22 | 2022-01-27 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Argon enhancing method and device |
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|---|---|---|---|---|
| EP3700857B1 (en) | 2017-10-24 | 2021-12-15 | Linde GmbH | Method and apparatus for treating a sour gas mixture |
| EP3727646B1 (en) | 2017-12-19 | 2023-05-24 | Linde GmbH | Gas treatment method including an oxidative process providing waste heat and corresponding apparatus |
| EP3557166A1 (en) | 2018-04-19 | 2019-10-23 | Linde Aktiengesellschaft | Method for the low-temperature decomposition of air and air separation plant |
| US20200080773A1 (en) * | 2018-09-07 | 2020-03-12 | Zhengrong Xu | Cryogenic air separation unit with flexible liquid product make |
| WO2020083527A1 (en) | 2018-10-23 | 2020-04-30 | Linde Aktiengesellschaft | Method and unit for low-temperature air separation |
| WO2020160842A1 (en) | 2019-02-07 | 2020-08-13 | Linde Gmbh | Gas treatment method and apparatus including an oxidative process for treating a sour gas mixture using gas from an air separation process |
| JP2024013252A (en) * | 2022-07-20 | 2024-02-01 | 大陽日酸株式会社 | Heat exchanger |
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Also Published As
| Publication number | Publication date |
|---|---|
| RU2016147701A (en) | 2018-06-07 |
| CN107131718B (en) | 2020-12-22 |
| AU2016269434B2 (en) | 2022-03-31 |
| EP3179187B1 (en) | 2019-01-30 |
| EP3179186A1 (en) | 2017-06-14 |
| BR102016028677B1 (en) | 2022-08-16 |
| BR102016028677A2 (en) | 2017-07-25 |
| AU2016269434A1 (en) | 2017-06-22 |
| PL3179187T3 (en) | 2019-07-31 |
| CL2016003150A1 (en) | 2017-06-02 |
| EP3179187A1 (en) | 2017-06-14 |
| RU2016147701A3 (en) | 2020-04-14 |
| RU2722074C2 (en) | 2020-05-26 |
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