CN104246401B - For the method by separating air by cryogenic distillation - Google Patents
For the method by separating air by cryogenic distillation Download PDFInfo
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- CN104246401B CN104246401B CN201280016801.6A CN201280016801A CN104246401B CN 104246401 B CN104246401 B CN 104246401B CN 201280016801 A CN201280016801 A CN 201280016801A CN 104246401 B CN104246401 B CN 104246401B
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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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
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- 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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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- 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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- 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
- F25J3/04181—Regenerating the adsorbents
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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
- F25J3/04248—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
- F25J3/04296—Claude expansion, i.e. expanded into the main or 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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
- F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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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
- F25J3/04472—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
- F25J3/04478—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for controlling purposes, e.g. start-up or back-up procedures
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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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
- F25J2205/72—Pressurising or depressurising the adsorption vessel
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
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- Separation By Low-Temperature Treatments (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
In airdistillation method, the air be cleaned is exchanging cooling in pipeline (8) and is being sent to the destilling tower (12) of Tower System subsequently, and only during pressure period again, extracts oxygen-rich fluid and nitrogen-rich stream from the tower (14) of Tower System.Be formed in compressor and be used to pressurize to the absorber completing its regeneration stage at least in part by the air stream through purification between the 3%-20% of air that compresses, and in compressor, be substantially equal at absorber pressure dwell in compressor by the air mass flow compressed by the air mass flow compressed during absorption phase.A part through the air of purification is sent to turbine (27), this portion of air reduces pressure and is sent to subsequently in air in this turbine, to guarantee that it is retained to small part cooling in whole cycle period, and the amount being sent to the reduced pressure air stream of air at the pressure dwell of absorber is less than the amount being sent to air during the absorption phase of same absorber.
Description
The present invention relates to a kind of for being separated air by airdistillation, in particular for producing the method for oxygen and/or nitrogen and/or argon, in the method, air to be distilled is cleaned in advance by least two absorbers, described each absorber follows a circulation with staggering in time, the regeneration stage that wherein said circulation is experienced the absorption phase under the pressure of this circulation successively and stopped with the pressurization of absorber.
The pressure related to herein is absolute pressure.
In the equipment of this type, the distillation of the air compressed by compression set in advance performs under low temperature/cryogenic temperature, therefore require that this air of purification is to remove the composition (that is, mainly water and carbon dioxide) of solidification temperature higher than the vapo(u)rizing temperature of air from air.The main purpose of air distillation provides oxygen and/or nitrogen with liquid and/or gaseous form.This production creates the fluid (such as dirty nitrogen, is called as residual nitrogen) with low oxygen content of liquid state or gaseous form and the co-production of high-purity nitrogen.
The purification of air to be distilled is arranged on adsorbent on bed and alternate cycles ground two bottles operating and adsorptive hindrance becomes to assign to perform by accommodating usually.When a bottle is in absorption phase, that is, it purifies air to be distilled, another bottle is in regeneration stage, that is, it is utilized dry regeneration gas (such as, residual nitrogen) to rinse, release/desorb deposits impurity on the sorbent during its previous absorption phase.When the regeneration of adsorbent is at high temperature and when under low pressure implementing relative to the pressure kept between adsorption cycle, the regeneration effect of adsorbent strengthens, this requires the bottle pressurization to the regeneration stage terminating it, to recover gratifying pressure condition for its next absorption phase.
For this reason, prior art is included in absorption phase and extracts the sub-fraction that purifies air in the exit of bottle and at the end of regeneration stage, make it be decompressed in bottle, to increase the pressure of the latter.But during this operation, indispensable is that to keep being conveyed to the air mass flow of distillation constant, to prevent any fluctuation in the supply of distilling apparatus and for keeping the production of oxygen and/or nitrogen and/or argon.Like this, at each pressure dwell again, air compression plant must provide the air for pressurizeing of this surplus.But this extra air mass flow means that compression set exceeds size and thus extra cost.The nominal air flow that certain needs provide bottle handled in absorption for the bottle of general size the pressurization of about 15 minutes duration about 5% additional compressed air stream (optimization according to circulation).
Therefore, outside the pressurization duration, compression set is with the operation of nominal air flow, that is, it corresponds to the separating power for separating of the equipment of air.
So for 100kNm
3the maximum compression machine flow of/h, the normal flow rate used will be the 95kNm being sent to ice chest (distillation is carried out) wherein
3/ h, and 100kNm
3/ h is only used for single pressure period, wherein 5kNm when regeneration ending
3the air of/h is transferred so that in pressurized bottle one.
Certain methods for separating of air uses loss air system, and the air be wherein all cleaned is not sent to destilling tower.In this case, generally there is expansion turbine, it is decompressed to making the excess air relevant with oxygen demand close to atmospheric pressure.
In such method, preferably do not implement the conventional pressure method of absorber.
The object of the invention is by reducing, even avoiding the oversize of compressor by eliminating increase air mass flow to be compressed to provide the additional gas needed for the pressurization of the bottle of adsorbent.
For this purpose, the present invention advises a kind of for air distillation, in particular for producing the method for oxygen and/or nitrogen and/or argon, air wherein to be distilled is compressed in advance in compressor, be cleaned by least two absorbers, each absorber follows a circulation with staggering in time, and the high pressure (P in this circulation is experienced in wherein said circulation successively
ads) under absorption phase and at low pressure P
atmosunder the regeneration stage stopped with the pressure period again of described absorber, the air be cleaned cools and is sent to the destilling tower of Tower System subsequently in exchange pipeline, and oxygen-rich fluid and nitrogen-rich stream are extracted by the tower from described Tower System, only during the described pressure period again, be formed in described compressor and be used to pressurize to the absorber completing its regeneration stage at least in part by the air stream through purification between the 3-20% of air that compresses, and in described compressor, be substantially equal at described absorber pressure dwell described compressor in by compress air mass flow by the air mass flow compressed in absorption phase, it is characterized in that, the portion of air of the described air be cleaned is sent to turbine, wherein said portion of air expands and is sent to air subsequently to provide cryogenic conditions at least in part in whole cycle period, and the expanded air flow being sent to air at the pressure dwell of absorber was less than during the absorption phase of same absorber, is even sent to the expanded air flow of air during all the other stage except the pressure period of circulation.
Term " be substantially equal to " cover wherein during absorption phase in compressor by the air capacity compressed with differed at the most 5% by the air mass flow compressed in compressor at absorber pressure dwell, preferred at the most 3% situation.More preferably two air mass flows are strictly equal.
According to the further feature of this method, employing or the combination according to technically permission separately:
-during the absorption phase of absorber, in described compressor, equaled at this absorber pressure dwell in this compressor by the air mass flow compressed by the air mass flow compressed;
-be sent to turbine and the minimizing being sent to the air mass flow of air subsequently equals to use with the air mass flow of the absorber pressurization to pressure period that completes it again at described pressure dwell again at pressure dwell again;
-the amount that is sent to the air of distilling apparatus is constant in whole cycle period;
-be sent to turbine and the minimizing being sent to the air mass flow of air is subsequently less than and uses with the air mass flow of the absorber pressurization to pressure period that completes it again at pressure dwell again at the pressure dwell of absorber;
-during pressure period again, the air mass flow compressed in described compressor adds relative to the flow be transferred during all the other stages of circulation, and the amount being transported to the air of distilling apparatus keeps equal with the amount of the air be transferred during all the other stages of circulating;
-liquid stream is produced as final products;
-described purification method is the absorption of PSA, TSA or TPSA type;
-air expands and is sent to the tower of described Tower System in turbine;
-described Tower System is made up of the double tower comprising medium pressure column and lower pressure column;
-oxygen-rich stream is extracted from lower pressure column and is evaporated in exchange pipeline.
Represent " pressure-variable adsorption " with term " PSA " in this article.Represent " Temp .-changing adsorption " with term " TSA " in this article.Represent " alternating temperature pressure-variable adsorption " with term " TPSA " in this article.
When reading the following description only provided by way of example and with reference to appended accompanying drawing, the present invention will be understood better, wherein:
-Fig. 1 is the schematic diagram for operating the equipment according to method of the present invention.
Fig. 1 illustrates according to the equipment 1 for air distillation of the present invention.This equipment is such as the production of gaseous oxygen OG, and liquid oxygen OL.
Equipment 1 mainly comprises:
-air compressor 4;
-for by adsorbing the purifier 6 purified air, described purifier comprises two absorbers 7A, 7B of the form being rendered as two bottles on the one hand, each absorber accommodates the sorbing material (such as, may have the molecular sieve of aluminium oxide/alumina) that can adsorb and be present in water in air and carbon dioxide; On the other hand comprise pipeline and connection valve, arranging in the description of the described method can implemented in device 1 of described pipeline and connection valve clearly manifests and makes it possible to continuously each absorber 7A, 7B be presented to air stream to be distilled and the regeneration gas of adsorbent;
-loss air turbine 27;
-cold compressor 3;
-air is delivered to Cloud (Claude) turbine 5 of medium pressure column;
-main heat exchange pipe 8;
-for air distillation, the device 10 being rendered as double tower form, it evaporator-condenser 16 comprising medium pressure column 12, lower pressure column 14 and connect these two towers, and argon knockout tower 26; With
-for the reservoir 18 of storing liquid oxygen.
The operation of the distillation equipment 1 of Fig. 1 is as follows.
The to be distilled air compressed by compressor 4 is in advance cleaned absorber one of 7A, 7B purification of device 6, is then cooled to medium temperature by main heat exchange pipe 8.Absorption can be TSA(Temp .-changing adsorption), PSA(pressure-variable adsorption) or TPSA(alternating temperature pressure-variable adsorption) type.A part 25 for air is sent to loss air turbine 27, and the air expanded is sent to air after reheating in interchanger 8.Remaining air continues cooled.Another part 29 of air is sent to cold compressor 3, is sent back to and exchanges pipeline 8.Press to form expansion flow 7 during the part of supercharging stream is expanded in turbine 5.The expansion flow 7 be near its dew point is guided in the storage tank of medium pressure column 12.All the other pressurized airs 9 continue in exchange pipeline 8 cooled, expand, be then sent to the centre position of medium pressure column 12 in valve V.
Evaporator-condenser 16 is by making the liquid oxygen of the storage tank of lower pressure column 14 (such as having the purity of 99.5%) evaporate at the top condensing gaseous nitrogen of medium pressure column 12.
" rich solution " LR(oxygen-enriched air extracted in the storage tank of medium pressure column 12) after expanding, be injected into the centre position of lower pressure column 14, and substantially pure liquid nitrogen NL extracts on the top of medium pressure column 12, to be supplied to the top of reservoir 22 and lower pressure column 14.Liquid nitrogen and/or liquid oxygen are produced as final products, are sent to client in liquid form.
The not purity nitrogen extracted from the top of lower pressure column 14 or " remnants " nitrogen NR are sent back to main heat exchange pipe 8, cause the cooling of air to be distilled herein.
Liquid oxygen OL is extracted by the storage tank from lower pressure column 14 and is supplied to and stores reservoir 18.In pump P after pressurization, described liquid oxygen evaporates and is equipped with formation pressurized gaseous oxygen by product pipeline 32 points in main heat exchange pipe 8.
Argon is produced tower 26 and is supplied by lower pressure column 14.
Except the operation (it meets the pressures cycle along with the time of Fig. 2) of purifier 6, the operation of the described distillation equipment described can be implemented continuously.But according to customer demand, power cost etc., all fluids can by discontinuous production.
The circulation of Fig. 2 comprises 4 successive stages I to IV, illustrates, equals about 360 minutes for the cycle being substantially equal to circulate described in the adsorptive pressure of 20bar.
For absorber 7A, this 4 steps will be described successively, absorber 7B should be understood and follow these identical steps by opening or closing of connection valve with the time delay of T/2 substantially, described connection valve represents with the Reference numeral that those Reference numerals with absorber 7A are identical, and wherein alphabetical A is replaced by letter b and the state (opening/closing) of each valve will be contrary (close/open).
During step 1, that is, t=0 to t=T/2, absorber 7A is in and is expressed as P
adshigh operating pressure under absorption phase, and absorber 7B is in regeneration stage.Absorber 7A is supplied to by the valve 40A opened by the air that compressor 4 compresses.The outlet of absorber 7A is connected to by the valve 42A opened and exchanges pipeline 8.
During Step II, III and IV, absorber 7A is in regeneration stage, and absorber 7B is in absorption phase.More accurately, during Step II, to open to the valve 44A that air ventilates for making absorber 7A and make the pressure of the inside of the bottle of absorber 7A be substantially equal to be expressed as P in the drawings
atmoatmospheric pressure.
During Step II I, valve 44A stays open and extracts on the top of lower pressure column 14, then in interchanger 8, is supplied to absorber 7A by the residual nitrogen NR heated by the valve 46A opened, with circulated in countercurrent wherein.This is effective stage of regeneration, and during this stage, impurity is released and the regeneration of (adsorbent) bed.During step IV, valve 44A and 46A closes, and pressurizes to allow absorber.In a first step, that is, during the first sub-step IV', the pressurization of absorber is provided by the valve 42A opened by the air stream purified, and this air stream purified is from bottle 7A, 7B.Sub-step IV' is by sub-step IV " to continue, until the pressure in absorber 7A is substantially equal to high pressure P by opening valve 50
ads.
By method according to the present invention, during step IV, the pressurization of each absorber no longer requires the flow increasing compressor 4.So, compressor is sizing in the best way, namely with the mode sizing of its metered flow substantial constant.Relative to those compression sets of the equipment involved by prior art, reduce for the investment of this compression set and running cost.
During absorption phase, compressor 4 compresses 100kNm
3the air of/h and the air all purified are sent to and exchange pipeline 8.30kNm
3the air of/h is sent to loss air turbine 5.70kNm
3the air of/h is sent to distillation column system.
During pressure period at the end of regeneration stage, compressor 4 compresses 100kNm
3the air of/h, 95kNm
3the air of/h is sent to and exchanges pipeline 8,5kNm
3the air of/h is transferred to pressurize to absorption bottle.25kNm
3the air of/h (therefore lacks 5kNm
3/ h) be sent to loss air turbine 5,70kNm
3the air of/h is still sent to distillation column system.
Should be understood that the present invention can be applied to any method relating to loss air turbine, no matter whether there is the compression in cold compressor, whether there is double tower, whether there is the production of argon, whether there is pressurization and the evaporation of liquid oxygen.
It is also to be understood that, if the minimizing of loss air mass flow is less than the flow being conveyed to pressurization, so must to increase by the flow that compresses at pressure dwell and the air mass flow be distilled remains unchanged, or less air will be conveyed to distillation and will be remained unchanged by the flow compressed.
Claims (14)
1. the method for air distillation, air wherein to be distilled is compressed in advance in compressor (4), by at least two absorber (7A, 7B) be cleaned, described each absorber follows a circulation with staggering in time, and the high pressure (P in this circulation is experienced in wherein said circulation successively
ads) under absorption phase and at low pressure P
atmosunder the regeneration stage stopped with the pressure period again of described absorber, the air be cleaned is cooled and is sent to the medium pressure column (12) of Tower System subsequently in exchange pipeline (8), and extract oxygen-rich fluid and nitrogen-rich stream from the lower pressure column (14) of described Tower System, only during the described pressure period again, be formed in described compressor and be used to pressurize to the absorber completing its regeneration stage at least in part by the air stream be cleaned between the 3-20% of air that compresses, and during absorption phase, in described compressor, be substantially equal at described absorber pressure dwell in described compressor by the air mass flow compressed by the air mass flow compressed, it is characterized in that, a part for the described air be cleaned is sent to turbine (27), a described part expands and is sent to air subsequently to provide cryogenic conditions at least in part in whole cycle period in described turbine, and the expanded air flow being sent to air at the pressure dwell of absorber is less than the expanded air flow being sent to air during the absorption phase of same absorber.
2. method according to claim 1, is characterized in that, the expanded air flow being sent to air at the pressure dwell of absorber is less than the expanded air flow being sent to air during all the other stages except the pressure period of circulation.
3. method according to claim 1 and 2, is characterized in that, during the absorption phase of absorber, equaled pressure dwell at this absorber in this compressor by the air mass flow compressed in described compressor (4) by the air mass flow compressed.
4. method according to claim 1 and 2, it is characterized in that, be sent to described turbine (27) and the minimizing being sent to the air mass flow of air subsequently equals to use with the air mass flow of the absorber pressurization to pressure period that completes it again at described pressure dwell again at pressure dwell again.
5. method according to claim 4, is characterized in that, is transferred so that the amount of the air distilled is constant in whole cycle period.
6. method according to claim 1 and 2, it is characterized in that, be sent to described turbine (27) and the minimizing being sent to the air mass flow of air is subsequently less than and uses with the air mass flow of the absorber pressurization to pressure period that completes it again at pressure dwell again at the pressure dwell of absorber.
7. method according to claim 6, it is characterized in that, during pressure period again, in described compressor (4), the air mass flow of compression adds relative to the flow be transferred during all the other stages of described circulation, and is transferred so that the amount of the air distilled keeps equaling the amount of the air be transferred during all the other stages of described circulation.
8. method according to claim 1 and 2, is characterized in that, liquid stream (22) is produced as final products.
9. method according to claim 1 and 2, is characterized in that, purification method is the absorption of PSA, TSA or TPSA type.
10. method according to claim 1 and 2, is characterized in that, air expands and is sent to the tower of described Tower System in the second turbine (5).
11. methods according to claim 1 and 2, is characterized in that, the expanded air flow being sent to air at the pressure dwell of absorber is less than the expanded air flow being sent to air during all the other stages except any pressure period of circulation.
12. methods according to claim 1 and 2, is characterized in that, described Tower System is made up of the double tower (10) comprising medium pressure column (12) and lower pressure column (14).
13. methods according to claim 12, is characterized in that, extract oxygen-rich stream and make it evaporate in described exchange pipeline (8) from described lower pressure column (14).
14. methods according to claim 1, is characterized in that, described method is for the production of oxygen and/or nitrogen and/or argon.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR1152733 | 2011-03-31 | ||
| FR1152733A FR2973486B1 (en) | 2011-03-31 | 2011-03-31 | AIR SEPARATION METHOD BY CRYOGENIC DISTILLATION |
| PCT/FR2012/050587 WO2012131231A2 (en) | 2011-03-31 | 2012-03-21 | Method for separating air by means of cryogenic distillation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104246401A CN104246401A (en) | 2014-12-24 |
| CN104246401B true CN104246401B (en) | 2016-02-03 |
Family
ID=45974440
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201280016801.6A Expired - Fee Related CN104246401B (en) | 2011-03-31 | 2012-03-21 | For the method by separating air by cryogenic distillation |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US20140013798A1 (en) |
| EP (1) | EP2712419B1 (en) |
| CN (1) | CN104246401B (en) |
| FR (1) | FR2973486B1 (en) |
| WO (1) | WO2012131231A2 (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2016025834A1 (en) * | 2014-08-15 | 2016-02-18 | Biomerieux, Inc. | Methods, systems, and computer program products for detecting a surface using a pipette and/or positioning a pipette |
| US10401083B2 (en) * | 2015-03-13 | 2019-09-03 | Linde Aktiengesellschaft | Plant for producing oxygen by cryogenic air separation |
| US10895417B2 (en) | 2016-03-25 | 2021-01-19 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for the production of air gases by the cryogenic separation of air with improved front end purification and air compression |
| FR3074274B1 (en) * | 2017-11-29 | 2020-01-31 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
| US11029086B2 (en) * | 2018-12-21 | 2021-06-08 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and apparatus for reducing process disturbances during pressurization of an adsorber in an air separation unit |
| US11137205B2 (en) * | 2018-12-21 | 2021-10-05 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and apparatus for eliminating heat bumps following regeneration of adsorbers in an air separation unit |
| CN110787587A (en) | 2019-11-08 | 2020-02-14 | 乔治洛德方法研究和开发液化空气有限公司 | Air separation purification pressure equalizing system and control method |
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| JPS52124468A (en) * | 1976-04-14 | 1977-10-19 | Kobe Steel Ltd | Raw air flowing volume regulation of air separator |
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| FR2913759B1 (en) * | 2007-03-13 | 2013-08-16 | Air Liquide | METHOD AND APPARATUS FOR GENERATING GAS AIR FROM THE AIR IN A GAS FORM AND LIQUID WITH HIGH FLEXIBILITY BY CRYOGENIC DISTILLATION |
| US20110197630A1 (en) * | 2007-08-10 | 2011-08-18 | L'air Liquide, Societe Anonyme Pour L'etude Et L'e Xploitation Des Procedes Georges Claude | Process and Apparatus for the Separation of Air by Cryogenic Distillation |
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2011
- 2011-03-31 FR FR1152733A patent/FR2973486B1/en not_active Expired - Fee Related
-
2012
- 2012-03-21 CN CN201280016801.6A patent/CN104246401B/en not_active Expired - Fee Related
- 2012-03-21 EP EP12714821.1A patent/EP2712419B1/en not_active Not-in-force
- 2012-03-21 WO PCT/FR2012/050587 patent/WO2012131231A2/en active Application Filing
- 2012-03-21 US US14/004,264 patent/US20140013798A1/en not_active Abandoned
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| US6073463A (en) * | 1998-10-09 | 2000-06-13 | Air Products And Chemicals, Inc. | Operation of a cryogenic air separation unit which intermittently uses air feed as the repressurization gas for a two bed PSA system |
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Also Published As
| Publication number | Publication date |
|---|---|
| WO2012131231A3 (en) | 2015-08-20 |
| WO2012131231A2 (en) | 2012-10-04 |
| EP2712419A2 (en) | 2014-04-02 |
| FR2973486B1 (en) | 2013-05-03 |
| FR2973486A1 (en) | 2012-10-05 |
| CN104246401A (en) | 2014-12-24 |
| US20140013798A1 (en) | 2014-01-16 |
| EP2712419B1 (en) | 2017-08-09 |
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