CN102741636A - Method and device for producing a gaseous pressurized oxygen product by cryogenic separation of air - Google Patents
Method and device for producing a gaseous pressurized oxygen product by cryogenic separation of air Download PDFInfo
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- CN102741636A CN102741636A CN2010800357860A CN201080035786A CN102741636A CN 102741636 A CN102741636 A CN 102741636A CN 2010800357860 A CN2010800357860 A CN 2010800357860A CN 201080035786 A CN201080035786 A CN 201080035786A CN 102741636 A CN102741636 A CN 102741636A
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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
- F25J3/04006—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
- 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
- F25J3/04066—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 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
- F25J3/04006—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
- F25J3/04248—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.
- F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
- F25J2240/04—Multiple expansion turbines in parallel
Abstract
The invention relates to a method and a device used for producing a gaseous oxygen pressurized product by cryogenic separation of air in a distillation column system which has at least one separation column. Feed air is compressed in an air compressor. A first partial flow (2, 4, 6, 7) of the compressed feed air is expanded to perform work (5, 8). A second partial flow (3) of the compressed feed air (1) is cooled and liquefied or pseudo-liquefied and subsequently introduced into the distillation column system. A liquid oxygen product flow (51) is removed from the distillation column system, brought in the liquid state to a first elevated pressure (52), evaporated or pseudo-evaporated at said first elevated pressure by indirect heat exchange (10) with the second partial flow (3) of the compressed feed air, heated to approximately the ambient temperature (10) and finally drawn off in the form of a gaseous product flow (55). The evaporated or pseudo-evaporated oxygen product flow (53) is brought further to a second elevated pressure that is higher than the first elevated pressure in a cold compressor (13). The product flow (54) is heated under said second elevated pressure to approximately the ambient temperature (10). At least part of the mechanical energy generated during the work-performing expansion (5, 8) of the first partial flow (3) is used to drive the cold compressor (13).
Description
Technical field
The present invention relates to method according to the preamble of claim 1.
Background technology
In this process, place the oxygen product stream under the pressure relatively to evaporate with liquid state, and finally obtain as the gaseous state pressurized product with heat carrier.This method is also referred to as interior compression.It is used to obtain pressurised oxygen.For the situation of supercritical pressure, itself can not undergo phase transition, and " pseudo-evaporation " takes place product stream then.
With the product stream of (puppet) evaporation relatively, be in heat carrier high pressure under liquefy (perhaps being in supercritical pressure following time at it puppet takes place liquefies).Heat carrier forms through portion of air usually, under the situation of " the second portion stream " of the feeding air of compression.
Interior compression method is for example in DE 830 805, DE 901 542 (=US2,712,738/US2,784; 572), DE 952 908, DE 1 103 363 (=US3,083,544), DE 1 112 997 (=US3,214; 925), DE 1 124 529, DE 1 117 616 (=US3,280,574), DE 1 226 616 (=US3,216; 206), DE 1 229 561 (=US3,222,878), DE 1 199 293, DE 1 187 248 (=US3,371; 496), DE 1 235 347, DE 1 258 882 (=US3,426,543), DE 1 263 037 (=US3,401; 531), DE 1 501 722 (=US3,416,323), DE 1 501 723 (=US3; 500,651), DE 253 132 (=US4,279; 631), DE 2 646 690, EP 93 448 B1 (=US4,555,256), EP 384 483 B1 (=US5; 036,672), EP 505 812 B1 (=US5,263; 328), EP 716 280 B1 (=US5,644,934), EP 842 385 B1 (=US5; 953,937), EP 758 733 B1 (=US5,845; 517), EP 895 045 B1 (=US6,038,885), DE 198 03 437 A1, EP 949 471 B1 (=US6; 185,960B1), EP 955 509 A1 (=US6,196; 022B1), EP 1 031 804 A1 (=US6,314,755), DE 199 09 744 A1, EP 1 067 345 A1 (=US6; 336,345), EP 1 074 805 A1 (=US6,332; 337), DE 199 54 593 A1, EP 1 134 525 A1 (=US6,477,860), DE 100 13 073 A1, EP 1 139 046 A1, EP 1 146 301 A1, EP 1 150 082 A1, EP 1 213 552 A1, DE 101 15 258 A1, EP 1 284 404 A1 (=US2003/051504 A1), EP 1 308 680 A1 (=US6; 612,129B2), DE 102 13 212 A1, DE 102 13 211 A1, EP 1 357 342 A1 or DE 102 38 282 A1, DE 103 02 389 A1, DE 103 34 559 A1, DE 103 34 560 A1, DE 103 32 863 A1, EP 1 544 559 A1, EP 1 585 926 A1, DE 10 2,005 029 274 A1, EP 1 666 824 A1, open among EP 1 672 301 A1, DE 10 2,005 028 012 A1, WO2007/033838 A1, WO2007/104449 A1, EP 1 845 324 A1, DE 10 2,006 032 731 A1, EP 1 892 490 A1, DE 10 2,007 014 643 A1, A1, EP 2 015 012 A2, EP 2 015 013 A2, EP 2 026 024 A1, WO2009/095188 A2 or DE 10 2,008 016 355 A1.
Compression method has many advantages in these, but need provide a part of feeding air that is under the extra high pressure as heat carrier.Must consume corresponding energy in addition.
Summary of the invention
The objective of the invention is to, the method and the corresponding apparatus of aforementioned type is provided, it is to work in mode useful especially aspect the energy.
This purpose is that the characteristic through claim 1 realizes.
At this, be not to boost to product pressure (" second elevated pressure ") fully, but only a part is boosted, promptly until lower " first elevated pressure " with liquid state.Remaining boosts after (puppet) evaporation in cold still carrying out under the gaseous state.At first it be self-contradictory for this to look, because the major advantage of interior compression is by the replacement gaseous compressed of boosting with liquid state.In addition, through cooled compressed heat is introduced in this process, this heat can't be discharged as the low-cost cooling agent of situation utilization such as the cooling water of hot compression.
But, in category of the present invention, shown the advantage of this method, overcome desired shortcoming.Through being lower than (puppet) evaporating pressure of final pressure, can also correspondingly select the pressure of the second portion stream that heat is provided lower.In addition, in order to drive the mechanical energy that cooling compressor use itself produces in the method; The negative booster that the first that for this reason, especially for example will be used for feeding air through common axle or transmission device flows mechanically is connected directly to cooling compressor.But when the product stream through cooled compressed got into heat exchange once more, the shortcoming that the temperature of rising possibly occur also demonstrated advantage.Can get around the bottleneck in exchange diagram thus, and between feeding air to be cooled and backflow to be heated, realize especially effectively heat exchange generally.In category of the present invention, what cause thus further energy-conservationly just realizes the beat all energy consumption that significantly reduces.
For example for exceeding (puppet) evaporating temperature 2 to 50K of the product stream under first elevated pressure, preferred 5 to 10K for the inlet temperature of cooling compressor.When oxygen product pressure (" second elevated pressure ") is between 20 and 40 crust, said method advantageous particularly.The pressure ratio at cooling compressor place is preferably 1.4 to 2.1, and " first elevated pressure " is between 10 and 30 crust.
Said method can utilize single negative booster to implement basically.In the case, except cooling compressor, also must consumption-type brake, generator or thermocompressor be connected with negative booster, to produce the required refrigeration of this method.Optionally, can move second negative booster with appropriate process stream, this negative booster is born the task of refrigeration.
Preferably in two parallel connections or the negative booster that is connected in series, implement the acting decompression of first's stream.For example can one of two negative boosters be connected with cooling compressor in the case, another is connected with thermocompressor, generator or consumption-type brake.
When negative booster was connected in series, advantageously first's stream heated (middle heating) between two negative boosters.
When negative booster was connected in parallel, advantageously two negative boosters had identical inlet temperature and/or identical inlet pressure or identical outlet pressure and/or identical outlet temperature.
In a special embodiment of the present invention, the mechanical energy of two negative boosters is used to drive cooling compressor.Therefore two negative boosters mechanically are connected (and choose wantonly extra be connected with thermocompressor, generator or consumption-type brake) with cooling compressor.Replace one or two speedup turbine commonly used at this, use two turbines that are connected in series, they for example mechanically are connected to each other through common axle or driver.Particularly advantageously be, in common shell, have the structure of two turbine wheels, they drive common axle, so are unit.Common axle drives cooling compressor and optional another brake apparatus, for example consumption-type brake, generator or the thermocompressor of driving.
The heating of the evaporation of the liquefaction of advantageously, the cooling of feeding air, second portion stream or pseudo-liquefaction, product stream or pseudo-evaporation and product stream is implemented in main heat exchanger.Should " main heat exchanger " can constitute, for example constitute by one or more flat plate heat exchanger pieces by one or more parallel connections and/or the heat transfer section that is connected in series.
In addition, the invention still further relates to according to Claim 8 to 13 equipment through low temperature air separating generation gaseous state pressurized product.
Set forth the present invention and other details of the present invention in more detail by embodiment illustrated in the accompanying drawings below.Accompanying drawing only comprises the major part and the corresponding device thereof of this method, and air compressor and distillation column system particularly are not shown.The latter is preferably through being used for the double tower system formation commonly used that nitrogen oxygen separates.
Description of drawings
Shown in Figure 1 is first embodiment with ensemble machine of the present invention,
Fig. 2 to 5 is depicted as other embodiments, wherein only has a negative booster to drive cooling compressor separately.
The specific embodiment
Mutual corresponding components or method step have identical Reference numeral in institute's drawings attached.
In Fig. 1, air 1 flows out under very high pressure from main air compressor and air cleaning unit subsequently (both are all not shown), and is distributed into first's stream 2 (turbine flow) and second portion stream 3 (throttling valve flows).
Hot junction with first's stream 2 introducing main heat exchangers 10.Under the medium temperature first circulated that piping 4 extracts once more and subsequently in first turbine 5 acting be decompressed to intermediate pressure.Middle forced air 6 is heating once more (heat the centre) in main heat exchanger 10, and delivers to second turbine 8 through pipeline 7, and is decompressed to the operating pressure of the high-pressure tower that is approximately the distillation column system (not shown) from middle pressure acting at this.The waste gas 9 of second turbine 8 is delivered to high-pressure tower as the feeding air that is gaseous state basically.
Second portion stream 3 is guided through main heat exchanger 10 under very high pressure until cold junction; And be provided under pressure the heat of the oxygen product stream of evaporation or pseudo-evaporation at this; This oxygen product stream extracts from distillation column system with liquid (51-LOX), and in pump 52, is applied to " first elevated pressure " of 19.5 crust.(all the other backflows through main heat exchanger are not shown at this.) cold second portion stream is decompressed in choke valve 11 and is approximately high-pressure tower pressure, and with liquid or introduce one or more towers of distillation column system as biphase mixture.
Two turbines 5,8 mechanically connect through driving this two common axle 12.In addition, this axle is provided with cooling compressor 13, and this cooling compressor is to drive through the mechanical energy that in turbine, produces and be transferred on the axle 12.In addition, this axle also drives consumption-type brake, generator or thermocompressor (not shown).
The product stream 53 of evaporation extracts from main heat exchanger 10 being higher than under about 5 to 10K the medium temperature of (puppet) evaporating temperature, and delivers to cooling compressor 13.At this it further is compressed to " second elevated pressure " of 33 crust by " first elevated pressure ".It is discharged by cooling compressor (through pipeline 54) with the temperature that is higher than inlet temperature 15 to 30K, go up in place then and deliver to main heat exchanger 10 once more, and be heated at this and be approximately environment temperature.Extract gaseous state pressurized product (PGOX) through pipeline 55 by the hot junction at last.
In Fig. 2, two negative booster parallel connections are provided with.At this, first stream 4 is distributed into two tributaries 204,207 under medium temperature, only acting decompression in turbine 205,208 of these two each leisures of tributary.The air stream of this two stock-traders' know-hows decompression is merged once more, and continuation as shown in Figure 1 is through pipeline 9 guiding.
In addition, two turbines constitute with the mode of the machine of two separation.First turbine 205 drives thermocompressor 223 through the first common axle.This thermocompressor constitutes with the mode of the back compressor of the feeding air 1 that is used for compressing at unshowned air compressor.Aftercooler is set subsequently, and with postmenstruation air compressed deliver to the hot junction of main heat exchanger 10 through pipeline 201.Second turbine 208 drives the cooling compressor 13 of the product stream 53 that is used for (puppet) evaporation through the second common axle.
The difference of Fig. 3 and Fig. 2 is, is not that whole air 1 are implemented the later stage compression, but only second portion stream 303,3 is implemented the later stage compression.For this reason, the feeding air 1 that in air compressor, compresses had been distributed into first's stream 2 and second portion stream 303 before back compressor 323, and only second portion stream 303 was delivered to back compressor 323.At last, the second portion stream 3 that will compress postmenstruation is delivered to the hot junction of main heat exchanger 10 as previously mentioned, and forms the throttling valve flow.
In Fig. 4, demonstrate the scheme of another change of Fig. 2.At this, in one of main heat exchanger 10 extra pipeline group 410, cool off in advance at compressor 223 upper reaches, back through the feeding air of compression, as said more in detail among the DE 10 2,007 042 462.
In a similar fashion, the embodiment of Fig. 5 and the difference of Fig. 3 are, the extra pipeline group 510 of main heat exchanger.
Claims (13)
1. be used in the method for distillation column system through low temperature air separating generation gaseous oxygen pressurized product, this distillation column system has at least one knockout tower, wherein in the method,
-feeding air is compressed in air compressor,
-make first stream (2,4,6,7) acting decompression (5,8) through the feeding air of compression,
-will introduce subsequently in the distillation column system through second portion stream (3) cooling and the liquefaction or the pseudo-liquefaction of the feeding air (1) of compression,
-liquid oxygen product stream (51) is extracted from distillation column system; Be applied to first elevated pressure (52) with liquid condition; Through evaporating or pseudo-evaporation with the indirect heat exchange (10) through the second portion stream (3) of the feeding air of compression, heating (10) is to being approximately environment temperature under this first elevated pressure, and finally extracts as gaseous product flow (55); It is characterized in that
-will in cooling compressor (13), further be applied to second elevated pressure that is higher than first elevated pressure through the oxygen product stream (53) of evaporation or pseudo-evaporation, and
-product stream (54) is heated (10) to being approximately environment temperature, wherein under this second elevated pressure
-mechanical energy of at least a portion generation when (5,8) are reduced pressure in first's stream (3) acting is used to drive cooling compressor (13).
2. according to the method for claim 1, it is characterized in that the acting decompression of first stream (2,4,6,7) is implemented in two parallel connections or the negative booster (5,8) that is connected in series.
3. according to the method for claim 2, it is characterized in that first's stream (6) heats (10) between two negative boosters that are connected in series.
4. according to the method for claim 2, it is characterized in that two negative boosters that are connected in parallel have identical inlet temperature and/or identical inlet pressure.
5. according to the method for claim 4, it is characterized in that two negative boosters that are connected in parallel have identical outlet pressure and/or identical outlet temperature.
6. according to the method for claim 2 or 3, it is characterized in that, the mechanical energy of two negative boosters (5,8) is used to drive cooling compressor (13).
7. according to the method for one of claim 1 to 4, it is characterized in that the heating of the evaporation of the liquefaction of the cooling of feeding air, second portion stream or pseudo-liquefaction, product stream or pseudo-evaporation and product stream is implemented in main heat exchanger.
8. be used for producing through low temperature air separating the equipment of gaseous oxygen pressurized product, it has
-have a distillation column system of at least one knockout tower,
-be used to compress the air compressor of feeding air,
-be used to make do work first negative booster of decompression (5,8) of first's stream (2,4,6,7) through the feeding air of compression,
-be used to cool off and liquefy or pseudo-liquefaction through the device of the second portion stream (3) of the feeding air (1) of compression,
-be used for the device of introducing distillation column system through first's stream of liquefaction or pseudo-liquefaction,
-be used for extracting liquid oxygen product stream (51) from distillation column system; Be applied to first elevated pressure (52) with liquid condition; Under this first elevated pressure through with indirect heat exchange (10) evaporation or pseudo-evaporated liquor through the second portion stream (3) of the feeding air of compression, heating (10) is to being approximately environment temperature, and the device of finally discharging as gaseous product flow (55); It is characterized in that
-be used for flowing the cooling compressor (13) that (53) further boost to second elevated pressure that is higher than first elevated pressure through the oxygen product that makes evaporation or pseudo-evaporation with lower device,
-be used for product stream (54) is heated (10) to the device that is approximately environment temperature under this second elevated pressure,
-be used at least a portion is flowed the device that the mechanical energy that produces when (5,8) are reduced pressure in (3) acting is transferred to cooling compressor (13) in first.
9. according to Claim 8 equipment is characterized in that being used for second negative booster (8) of first's stream (2,4,6,7) acting decompression, and this second negative booster is parallelly connected with first negative booster (5) or be connected in series.
10. according to Claim 8 or 9 equipment, it is characterized in that being used for the device of heating (10) first stream (6) between two negative boosters that are connected in series.
11. to one of 10 equipment, it is characterized in that according to Claim 8 two negative boosters that are connected in parallel have identical inlet temperature, identical inlet pressure, identical outlet pressure and/or identical outlet temperature.
12., it is characterized in that being used for the mechanical energy of two negative boosters (5,8) is transferred to the device of cooling compressor (13) according to Claim 8 to one of 11 equipment.
13. to one of 12 equipment, it is characterized in that the heating of the evaporation of the liquefaction of the cooling of feeding air, second portion stream or pseudo-liquefaction, product stream or pseudo-evaporation and product stream is implemented in main heat exchanger according to Claim 8.
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE200920010874 DE202009010874U1 (en) | 2009-08-11 | 2009-08-11 | Device for producing a gaseous print product by cryogenic separation of air |
| DE202009010874.0 | 2009-08-11 | ||
| EP09013224.2 | 2009-10-20 | ||
| EP09013224 | 2009-10-20 | ||
| PCT/EP2010/004883 WO2011018207A2 (en) | 2009-08-11 | 2010-08-10 | Method and device for producing a gaseous pressurized oxygen product by cryogenic separation of air |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102741636A true CN102741636A (en) | 2012-10-17 |
Family
ID=43586561
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010800357860A Pending CN102741636A (en) | 2009-08-11 | 2010-08-10 | Method and device for producing a gaseous pressurized oxygen product by cryogenic separation of air |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US20120174625A1 (en) |
| EP (1) | EP2464937A2 (en) |
| CN (1) | CN102741636A (en) |
| RU (1) | RU2012108588A (en) |
| WO (1) | WO2011018207A2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112361716A (en) * | 2020-10-26 | 2021-02-12 | 乔治洛德方法研究和开发液化空气有限公司 | Method and device for producing high-pressure gas from an air separation plant |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2600090B1 (en) * | 2011-12-01 | 2014-07-16 | Linde Aktiengesellschaft | Method and device for generating pressurised oxygen by cryogenic decomposition of air |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1102701A (en) * | 1993-09-01 | 1995-05-17 | 乔治·克劳德方法的研究开发空气股份有限公司 | Process and installation for the production of gaseous oxygen and/or gaseous nitrogen under pressure |
| CN1229185A (en) * | 1998-01-22 | 1999-09-22 | 气体产品与化学公司 | Elevated pressure air separation process with use of waste expansion for compression of process stream |
| US20050132746A1 (en) * | 2003-12-23 | 2005-06-23 | Jean-Renaud Brugerolle | Cryogenic air separation process and apparatus |
| CN1784580A (en) * | 2003-05-05 | 2006-06-07 | 液体空气乔治洛德方法利用和研究的具有监督和管理委员会的有限公司 | Cryogenic distillation method and system for air separation |
| WO2008116727A2 (en) * | 2007-03-23 | 2008-10-02 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for the separation of air by cryogenic distillation |
| FR2915271A1 (en) * | 2007-04-23 | 2008-10-24 | Air Liquide | Air separating method, involves operating extracted nitrogen gas from high pressure column at pressure higher than pressure of systems operating at low pressure, and compressing gas till pressure is higher than high pressure of systems |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4796431A (en) * | 1986-07-15 | 1989-01-10 | Erickson Donald C | Nitrogen partial expansion refrigeration for cryogenic air separation |
| EP1767884A1 (en) * | 2005-09-23 | 2007-03-28 | L'Air Liquide Société Anon. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude | Process and apparatus for the separation of air by cryogenic distillation |
| DE102006012241A1 (en) * | 2006-03-15 | 2007-09-20 | Linde Ag | Method and apparatus for the cryogenic separation of air |
-
2010
- 2010-08-10 WO PCT/EP2010/004883 patent/WO2011018207A2/en active Application Filing
- 2010-08-10 US US13/389,862 patent/US20120174625A1/en not_active Abandoned
- 2010-08-10 EP EP10749468A patent/EP2464937A2/en not_active Withdrawn
- 2010-08-10 CN CN2010800357860A patent/CN102741636A/en active Pending
- 2010-08-10 RU RU2012108588/06A patent/RU2012108588A/en not_active Application Discontinuation
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1102701A (en) * | 1993-09-01 | 1995-05-17 | 乔治·克劳德方法的研究开发空气股份有限公司 | Process and installation for the production of gaseous oxygen and/or gaseous nitrogen under pressure |
| CN1229185A (en) * | 1998-01-22 | 1999-09-22 | 气体产品与化学公司 | Elevated pressure air separation process with use of waste expansion for compression of process stream |
| CN1784580A (en) * | 2003-05-05 | 2006-06-07 | 液体空气乔治洛德方法利用和研究的具有监督和管理委员会的有限公司 | Cryogenic distillation method and system for air separation |
| US20050132746A1 (en) * | 2003-12-23 | 2005-06-23 | Jean-Renaud Brugerolle | Cryogenic air separation process and apparatus |
| WO2008116727A2 (en) * | 2007-03-23 | 2008-10-02 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for the separation of air by cryogenic distillation |
| FR2915271A1 (en) * | 2007-04-23 | 2008-10-24 | Air Liquide | Air separating method, involves operating extracted nitrogen gas from high pressure column at pressure higher than pressure of systems operating at low pressure, and compressing gas till pressure is higher than high pressure of systems |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112361716A (en) * | 2020-10-26 | 2021-02-12 | 乔治洛德方法研究和开发液化空气有限公司 | Method and device for producing high-pressure gas from an air separation plant |
Also Published As
| Publication number | Publication date |
|---|---|
| EP2464937A2 (en) | 2012-06-20 |
| WO2011018207A3 (en) | 2014-03-13 |
| RU2012108588A (en) | 2013-09-20 |
| WO2011018207A2 (en) | 2011-02-17 |
| US20120174625A1 (en) | 2012-07-12 |
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