CN101268326A - Process and apparatus for the separation of air by cryogenic distillation - Google Patents
Process and apparatus for the separation of air by cryogenic distillation Download PDFInfo
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- CN101268326A CN101268326A CNA2006800349904A CN200680034990A CN101268326A CN 101268326 A CN101268326 A CN 101268326A CN A2006800349904 A CNA2006800349904 A CN A2006800349904A CN 200680034990 A CN200680034990 A CN 200680034990A CN 101268326 A CN101268326 A CN 101268326A
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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
- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04139—Combination of different types of drivers mechanically coupled to the same compressor, possibly split on multiple compressor casings
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—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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- 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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- 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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- 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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- F25J3/04—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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- 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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- Engineering & Computer Science (AREA)
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- Mechanical Engineering (AREA)
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- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
A process for separating air by cryogenic distillation in a column system comprising a high pressure column and a low pressure column comprises compressing all the feed air in a first compressor (1) to a first outlet pressure, sending a first part of the air at the first outlet pressure to a second compressor (3) and compressing the air to a second outlet pressure, cooling at least part of the air at the second outlet pressure in a heat exchanger (5) liquefying at least part of the air at the second outlet pressure and sending the liquefied air to at least one column of the column system wherein at least 50% of the liquefied air sent to the column system has been compressed in the second compressor, cooling a second part of the air (12) at the first outlet pressure in the heat exchanger and expanding at least part of the second part of the air in an expander (13) from the first outlet pressure to the pressure of a column (30, 31) of column system and sending the expanded air to that column, at least partially vaporizing an auxiliary fluid (6) , eventually further warming said auxiliary fluid in the heat exchanger, sending at least part of this auxiliary fluid to a third compressor (8) to a third outlet pressure, introducing at least part (9) of said auxiliary fluid at said third outlet pressure in the heat exchanger, cooling said auxiliary fluid and at least partially liquefying said auxiliary fluid, removing said auxiliary stream (10) from the heat exchanger and expanding (16) it to a fourth pressure level before reintroducing it in the heat exchanger where it will be partially vaporized as above- mentioned, removing liquid (20) from a column (31) of the column system and vaporizing the liquid by heat exchange in the heat exchanger.
Description
Technical field
The present invention relates to a kind of method and apparatus that is used for by separating air by cryogenic distillation.The present invention is specifically related to be used to produce the method and apparatus of hyperbaric oxygen and/or nitrogen.
Background technology
Gaseous oxygen by air separation equipment production is in about high pressure of 20 to 50bar usually.Basic distillation scheme is normally produced the double tower process of oxygen in the bottom with the lower pressure column of 1.4 to 4bar pressure operation.Must oxygen be compressed to higher pressure by oxygen compressor or by liquid pump pressure method.Because the safety problem relevant with oxygen compressor, at present most oxygen generating plant is all based on liquid pump pressure method.In order to make Liquid High Pressure Oxygen vaporization, need booster compressor that additional motor drives that a part of feeding air or nitrogen are risen to elevated pressures in the 40-80bar scope.Replaced oxygen compressor with supercharger in fact.
When attempting reducing the complexity of oxygen generating plant, wish to reduce the quantity of motor compressor driven.If can not use supercharger equipment performance is not had much affect, then can aspect energy consumption, reduce cost greatly.In addition, the air cleaning member that is used for traditional oxygen generating plant will be operated under the pressure of about 5-7bar, and this pressure is the pressure of high-pressure tower basically, also wish this boost in pressure to higher level so that the compacter and cost of equipment is lower.
As US-A-5, the cold compression method described in 475,980 provides a kind of technology that drives oxygen generating plant with single air compressor.In the method, air to be distilled cools off the booster compressor that drives by the decompressor by exhaust in the high-pressure tower of double tower process then and further compresses in main heat exchanger.By doing like this, the blowdown presssure of air compressor is in the scope of 15bar, and this is also quite favourable to clean unit.An inconvenience of this method is, increases owing to the additional flow circuit that is generally used for cold compression plant causes the size of main heat exchanger.Can reduce the size of interchanger by the temperature difference that increases heat exchanger.But this can cause inadequate power to use and higher compressor discharge pressure, improves its cost thus.Fig. 1 illustrates the prior art, has wherein added the oil brake required energy of refrigeration that dissipates.In bigger equipment, can use compressor and/or generator to replace oil brake.
In Fig. 1, all feeding air compress, purify and deliver to as stream 11 the warm end/temperature end of heat exchanger 5 in clean unit 2 in compressor 1.All feeding air are cooled to medium temperature, discharge and compression cold compressor 8 from heat exchanger as stream 7.Compressive flow 9 is sent back to heat exchanger, is cooled to a temperature and a separated into two parts that is lower than the inlet temperature of cold compressor 8 with a higher medium temperature.Stream 15 is delivered in Cloud (Claude) decompressor of being braked by compressor 8 and oil brake 13.The remainder 10 of air liquefies in heat exchanger and separated into two parts, and a part is delivered to high-pressure tower 30, and remainder 34 is delivered to lower pressure column 31.
Make 28 expansions of oxygen enriched liquid stream and deliver to lower pressure column from high-pressure tower.Make 29 expansions of nitrogen-rich liquid stream and deliver to lower pressure column from high-pressure tower.Take out high-pressure gaseous nitrogen 14 from the top of high-pressure tower and it is heated up to form product stream 24.Take out liquid oxygen 20 from the bottom of lower pressure column 31, deliver to heat exchanger 5 by pump 21 pressurizations and as stream 22, liquid oxygen is by vaporizing to form gaseous state pressurised oxygen 23 with forced air 10 heat exchanges in this heat exchanger.Take out top nitrogen-rich gas stream 25 from lower pressure column 31, it is heated up in heat exchanger 5, form stream 26 then.
Some multi-form cold compression methods have also been described in prior art such as US-A-5379598, US-A-5596885, US-A-5901576 and US-A-6626008.
In US-A-5379598, sub-fraction feeding air further compresses to produce the required pressurized stream of oxygen vaporization by cold compressor then by booster compressor.This method still has at least two compressors, and still operation under low pressure of clean unit.
In US-A-5596885, sub-fraction feeding air is further compression in warm supercharger, simultaneously to the further compression in cold supercharger of small part air.Air from two superchargers is liquefied, and the air of part process cold compression expands in Cloud's decompressor.
US-A-5901576 has described the layout of a plurality of cold compression schemes, and the expansion of the rich solution of the vaporization of this cold compression scheme use high-pressure tower bottom or the expansion of elevated pressure nitrogen drive cold compressor.In some cases, the cold compressor of also using motor to drive.These methods also use the feeding air under the pressure that is about high-pressure tower to operate, and also need booster compressor under most of situation.
US-A-6,626,008 have described a kind of cold compressor of using to improve the heat pump cycle of distillating method, and this distillating method is used to produce the oxygen that double evaporators oxygen is handled the low-purity of usefulness.These class methods also adopt low air pressure and booster compressor usually.
Summary of the invention
Therefore, the objective of the invention is by a kind of inconvenience that solves traditional handicraft in order to simplification compressibility and the solution that reduces the size of clean unit is provided.In addition, can also realize good power consumption like this.Therefore can reduce the total cost of production of oxygen generating plant.The main improvement of power consumption is owing to replace specific heat to cause the minimizing of cold compressor flow by main use latent heat.
All percentages of listing all are molar percentages.
According to the present invention, provide a kind of and be used in the method for the Tower System that comprises high-pressure tower and lower pressure column by separating air by cryogenic distillation, this method may further comprise the steps:
I) in first compressor, all feeding air are compressed to first outlet pressure;
The first that ii) will be in the air of first outlet pressure delivers to second compressor, and this part air is compressed to second outlet pressure;
At least a portion of iii) cooling off the air that is in second outlet pressure in heat exchanger is in the compressed air of the cooling of second outlet pressure with formation, liquefaction is at least a portion of the air of second outlet pressure, and liquefied air is delivered at least one tower of Tower System;
Iv) cooling is in the second portion of air of first outlet pressure in heat exchanger, and makes at least a portion of the second portion of described air expand into the pressure of the tower of Tower System from first outlet pressure in decompressor, and the air after will expanding is delivered to this tower;
V) from the tower of Tower System, take out liquid,, and in heat exchanger, make this vaporizing liquid by heat exchange to this liquid pressurization;
The auxiliary fluid of vi) vaporizing at least in part, described auxiliary fluid is further heated up, at least a portion of this auxiliary fluid is delivered to the 3rd compressor it is compressed to the 3rd outlet pressure, the at least a portion that will be in the described auxiliary fluid of described the 3rd outlet pressure is introduced heat exchanger, cool off described auxiliary fluid and the described auxiliary fluid that liquefies at least in part, from heat exchanger, take out described auxiliary flow, and described auxiliary flow is being introduced again heat exchanger to make it be expanded to the 4th stress level before the vaporization therein as mentioned above partly.
According to optional feature of the present invention:
-other air liquefies in heat exchanger under first pressure.
-Di three compressor compresses comprise the auxiliary fluid of at least a following gas: He, H
2, Ne, N
2, CO, Ar, O
2, CH
4, Kr, NO, Xe, CF
4, HCF
3, C
2H
4, C
2H
6, C
2F
6, C
3F
8, N
2O, CO
2
Its key component of-Di three compressor compresses comprises Ar, O
2, CH
4With at least a auxiliary fluid among the Kr.
According to another aspect of the present invention, provide a kind of equipment that is used for by separating air by cryogenic distillation, having comprised:
A) Tower System;
B) first, second and the 3rd compressor;
C) decompressor;
D) be used for air is delivered to first compressor is in first outlet pressure with formation compressed-air actuated pipeline;
E) first that is used for being in the air of first outlet pressure delivers to second compressor is in the air of second outlet pressure with formation pipeline;
F) heat exchanger is used at least a portion that is in the air of second outlet pressure is delivered to this heat exchanger is in the cooling of second outlet pressure with formation compressed-air actuated pipeline;
G) be used for taking out the pipeline that is in the liquefied air of second outlet pressure and is used for liquefied air is delivered at least one tower of Tower System from heat exchanger;
H) be used for the pipeline that takes out the second portion of the air be in first outlet pressure and be used at least a portion of the second portion of air is delivered to decompressor from heat exchanger;
I) be used for the air that expanded at decompressor is delivered to the pipeline of at least one tower of Tower System;
J) be used for being used at least a portion of this liquid is pressurizeed with the device of formation fluid under pressure from the pipeline of the tower taking-up liquid of Tower System, and the pipeline that is used at least a portion of this fluid under pressure is delivered to heat exchanger; And
K) kind of refrigeration cycle, this kind of refrigeration cycle comprise the 3rd compressor and second decompressor (16), be used for auxiliary fluid from the 3rd compressor deliver to heat exchanger pipeline, be used for auxiliary fluid from heat exchanger deliver to second decompressor pipeline, be used for pipeline that auxiliary fluid is delivered to the pipeline of heat exchanger and is used for auxiliary fluid is delivered to from heat exchanger the 3rd compressor from second decompressor.
According to other optional aspect of the present invention, described equipment can comprise additional decompressor and be used for the device of delivering to this additional decompressor with from the nitrogen or the air of the tower of Tower System.
In the case, one in second compressor and the 3rd compressor can link with decompressor, and in second compressor and the 3rd compressor another can link with additional decompressor.
In second compressor and the 3rd compressor at least one and air expander link.
Preferably, the first that is used for being in the air of first outlet pressure pipeline of delivering to second compressor is connected the centre position of heat exchanger.
Preferably, second compressor and the 3rd compressor are connected in series.
Decompressor can be selected from following group, and this group comprises that it exports the air expander that is connected with high-pressure tower, air expander, elevated pressure nitrogen decompressor and the low pressure nitrogen decompressor that its outlet is connected with lower pressure column.
Described equipment can comprise and be selected from following group additional decompressor, and this group comprises air expander that its outlet is connected with high-pressure tower, it exports air expander, elevated pressure nitrogen decompressor and the low pressure nitrogen decompressor that is connected with lower pressure column.
Preferably, in the Fu Jia decompressor and second decompressor and the 3rd decompressor links.
Description of drawings
Describe the present invention in detail with reference to Fig. 2,3,5 and 6, Fig. 4 and Fig. 7 below, Fig. 2,3,5 and 6 is expression process charts according to cryogenic air separation process of the present invention, Fig. 4 is an exchange diagram, and Fig. 7 illustrates the system of connections that is used for compressor and decompressor in the method according to the invention.
The specific embodiment
The air stream (stream 11) that in the embodiment of Fig. 2, atmosphere is by air compressor 1 compression and purify in clean unit 2, does not have impurity with generation--for example moisture that can solidify in low-temperature equipment and carbon dioxide--.The first of described air compresses with its pressure of further lifting in booster brake compressor (boosterbrake compressor) 3.Then, the first of this pressurization (stream 4) cooling in main heat exchanger 5 forms liquefied air stream (stream 27) with condensation, is fed at least one destilling tower after this liquefied air stream expands in valve.According to employed pressure, air can liquefy in main heat exchanger or in the main heat exchanger downstream.The auxiliary fluid mixture 6 of krypton (90%) and oxygen (10%) is introduced heat exchangers 5, it is vaporized in heat exchanger 5 and in the cold auxiliary gaseous flow under the temperature T 1 of mediating with generation that heats up a little after the vaporization.At least a portion of this cold auxiliary flow (stream 7) is delivered in the cold brake compressor 8 compression for 1 time to promote its pressure (stream 9) in temperature T.To flow 9 then and send heat exchanger back to 2 times in the temperature T that is higher than T1, and it be cooled off with condensation form liquefaction auxiliary flow (stream 10) in heat exchanger 5, this liquefaction auxiliary flow expands in valve 16 and flows 6 to form.If flowing 6 is two-phase fluids, then can increase phase-splitter, liquid phase is introduced heat exchanger 5 and gas phase 7 is mixed with stream.Stream 11 second portion (stream 12) cooling in heat exchanger 5 should be flowed 15 and deliver to decompressor 13 expansions with inlet temperature T3 to be formed stream 15, entered high-pressure tower then.Preferably, the power that uses decompressor 13 to produce drives booster brake compressor 3.The remainder of stream 12 is liquefied as stream 33 and is sent to high-pressure tower 30.Can extract nitrogen-rich gas 14 from high-pressure tower 30, heat up in heat exchanger 5 to form stream 17, this stream 17 expands in the decompressor 18 with inlet temperature T4 then.The power of decompressor 18 can be preferably used for driving cold booster brake compressor 8.The exhaust of decompressor 18 (stream 19) is the cold junction of Returning heat-exchanger 5 then, to reheat to flowing 24 near environment temperature to form.The pressure of the liquid oxygen product 20 that pump 21 will extract from lower pressure column 31 bottoms is elevated to desirable pressure, then pressurized oxygen 22 is delivered to heat exchanger 5 and is vaporized and heat to generate oxygen product 23.Double tower system is as it has high-pressure tower 30 and lower pressure column 31 about the patent of air separation technology or the double tower process of the traditional type described in the document many, and the two is by being positioned at the reboiler-condenser thermally coupled of lower pressure column bottom.Argon column can use to provide with double tower system and concentrate argon stream.
Said temperature T1, T2, T3 and T4 provide as preferred the setting.Hereinbefore, the arrangement from the hottest temperature to the coldest temperature is T2, T5, T1 and T3.According to the pressure of vaporized oxygen and the pressure of Tower System, the order that can change these temperature is so that the processing performance optimization.
It should be noted that booster brake compressor 3 is single-stage compressors, and usually provide as the part of decompressor-supercharger assembly, therefore, with independently or the booster compressor that drives of motor compare, its simple structure many and its cost structure is much lower.But if necessary, compressor 3 can be independently or the booster compressor that drives of motor.Depend on stream 4 and stream 23 pressure, compressor 8 can be have one to four level independently or the booster compressor that drives of motor.Compressor 8 can directly be driven with identical speed by decompressor 18 (perhaps decompressor 13) alternatively, or by gear drive/speed change gear so that the best performanceization of supercharger and decompressor.
The scope of the technological parameter of the embodiment of Fig. 2 is as follows:
The pressure of stream 11: about 9 to 17bar a
The pressure of stream 4: about 16 to 50bar a
The pressure of stream 9: about 5 to 20bar a under the situation of rich krypton mixture
T1 :-110 ℃ to-165 ℃ approximately
Can be by extracting the flow that some streams 12 reduce by booster brake compressor 8 compressions as liquefied air stream 33 alternatively.Like this, need less power to drive booster brake compressor 8, therefore can save power.The amount of the air that liquefies under first pressure should be more than 50% of the liquefied air of delivering to Tower System, and preferably no more than 40%, more preferably no more than 35%.
Replacing the nitrogen decompressor with air expander in air separation technology is common practise.The embodiment of Fig. 3 has described this layout: after first compressor, stream 11 part 12 cool off in heat exchanger 5 and a part of extracting this stream to form stream 50, will flow 50 and deliver to decompressor 52 expansions, enter lower pressure column 31 then.The power of decompressor 52 is preferably used for driving cold compressor 8.It should be noted that also can be chosen in and divide stream 12 before entering heat exchanger 5, and corresponding air stream is delivered to cooling in the independent passage in the heat exchanger 5, expanded in decompressor 52, enter tower then.Fig. 4 illustrates the exchange diagram corresponding to the method for Fig. 3.
Can as shown in Figure 5ly revise above-mentioned technology a little: the part of air 53 of the exhaust stream 54 of decompressor 13 is heated up, deliver to decompressor 52 then and expand, then enter lower pressure column in heat exchanger 5.In stream 54, exist under the situation of condensation, can extract the gas that is fed into decompressor 52 by increasing gas-liquid separator, or even the storage tank that uses high-pressure tower better as separator, in this case, extract the gas that is fed into decompressor at the storage tank place of high-pressure tower.
Under the situation of a large amount of high pressure nitrogen-rich gas of many needs product, use nitrogen-rich gas decompressor 18 no longer economical.On the contrary, as shown in Figure 6, can directly extract and produce nitrogen-rich gas 14 to produce nitrogen product 41 from high-pressure tower 30.In these cases, the pressure that can select to promote compressor 1 is exported with the power that increases decompressor 13, thereby compensation is by the refrigeration deficiency of not using the nitrogen decompressor to cause.In order further to simplify the layout of decompressor and booster brake compressor, can mechanically be integrated into the decompressor and the booster brake (booster brake) of series connection in the individual system: two compressor brakes 3 of the power drive of decompressor 13 (single-stage) and 8 (two-stages).In addition, motor and/or generator 60 can be wished the performance that obtains from equipment and output is extracted or add machine power to system constantly according to certain from system.According to the flow and the pressure of decompressor and booster brake compressor, can use speed changer (gear drive) to make the systematic function optimization.Fig. 7 illustrates the layout with gear drive.Also can add this type systematic to other decompressor 18,52.
Can revise described method, make the liquid nitrogen vaporization of extraction become additional stream or the stream of the oxygen flow that replaces extracting.
Illustrated method illustrates double tower system, but can easily understand, and the present invention can be applicable to three-tower system.
Under the situation that double tower or three-tower system are under high pressure operated, some low pressure nitrogen can expand in decompressor 18.
Claims (8)
1. one kind is used for may further comprise the steps in the method for the Tower System that comprises high-pressure tower and lower pressure column by separating air by cryogenic distillation:
I) in first compressor (1), all feeding air are compressed to first outlet pressure;
The first (4) that ii) will be in the air of first outlet pressure delivers to second compressor (3), and this part air is compressed to second outlet pressure;
Iii) in heat exchanger (5), cool off at least a portion of the air that is in second outlet pressure;
Iv) in heat exchanger, cool off the second portion (12) of the air that is in first outlet pressure, and make at least a portion of the second portion of described air expand into the pressure of the tower (30) of Tower System from first outlet pressure in decompressor (13), and the air after will expanding is delivered to this tower;
V) from the tower (31) of Tower System, take out liquid (20),, and in heat exchanger, make this vaporizing liquid by heat exchange to this liquid pressurization;
The auxiliary fluid of vi) in heat exchanger, vaporizing at least in part, described auxiliary fluid is further heated up, at least a portion of this auxiliary fluid is delivered to the 3rd compressor (8) it is compressed to the 3rd outlet pressure, the at least a portion (9) that will be in the described auxiliary fluid of described the 3rd outlet pressure is introduced heat exchanger, cool off described auxiliary fluid and the described auxiliary fluid that liquefies at least in part, from heat exchanger, take out described auxiliary flow, and described auxiliary flow (6) is being introduced again heat exchanger to carry out making it be expanded to the 4th stress level before the aforementioned step of vaporizing at least in part.
2. method according to claim 1 is characterized in that, cools off at least a portion of the first of air in the upstream of second compressor (3).
3. method according to claim 2 is characterized in that, cools off at least a portion of the first of air in heat exchanger (5) in the upstream of second compressor (3).
4. method according to claim 2 is characterized in that, uses at least a portion of the first of refrigeration unit cooling air in heat exchanger in the upstream of second compressor.
5. according to the described method of claim 1 to 4, it is characterized in that other air (27,33) liquefies under at least one pressure in first pressure and second pressure in heat exchanger.
6. according to the described method of claim 1 to 5, it is characterized in that the 3rd compressor compresses is selected from the auxiliary fluid that comprises at least a group in the following gas: He, H
2, Ne, N
2, CO, Ar, O
2, CH
4, Kr, NO, Xe, CF
4, HCF
3, C
2H
4, C
2H
6, C
2F
6, C
3F
8, N
2O, CO
2
7. method according to claim 6 is characterized in that the key component of auxiliary fluid is Ar, O
2, CH
4At least a with among the Kr.
8. equipment that is used for by separating air by cryogenic distillation comprises:
A) Tower System (30,31);
B) first, second and the 3rd compressor (1,3,8);
C) first decompressor (13);
D) be used for air is delivered to first compressor is in first outlet pressure with formation compressed-air actuated pipeline;
E) first that is used for being in the air of first outlet pressure delivers to second compressor is in the air of second outlet pressure with formation pipeline;
F) heat exchanger (5) is used at least a portion that is in the air of second outlet pressure is delivered to this heat exchanger is in the cooling of second outlet pressure with formation compressed-air actuated pipeline;
G) be used for taking out the pipeline that is in the liquefied air of second outlet pressure and is used for liquefied air is delivered at least one tower of Tower System from heat exchanger;
H) be used for the pipeline that takes out the second portion of the air be in first outlet pressure and be used at least a portion of the second portion of air is delivered to decompressor from heat exchanger, be used for the air that expanded at decompressor is delivered to the pipeline of at least one tower of Tower System;
I) be used for being used at least a portion of this liquid is pressurizeed with the device of formation fluid under pressure from the pipeline of the tower taking-up liquid of Tower System, and the pipeline that is used at least a portion of this fluid under pressure is delivered to heat exchanger; And
J) kind of refrigeration cycle, this kind of refrigeration cycle comprise the 3rd compressor and second decompressor (16), be used for auxiliary fluid from the 3rd compressor deliver to heat exchanger pipeline, be used for auxiliary fluid from heat exchanger deliver to second decompressor pipeline, be used for pipeline that auxiliary fluid is delivered to the pipeline of heat exchanger and is used for auxiliary fluid is delivered to from heat exchanger the 3rd compressor from second decompressor.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP05108826A EP1767884A1 (en) | 2005-09-23 | 2005-09-23 | Process and apparatus for the separation of air by cryogenic distillation |
| EP05108826.8 | 2005-09-23 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101268326A true CN101268326A (en) | 2008-09-17 |
Family
ID=35809642
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2006800349904A Pending CN101268326A (en) | 2005-09-23 | 2006-09-21 | Process and apparatus for the separation of air by cryogenic distillation |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US20080223075A1 (en) |
| EP (2) | EP1767884A1 (en) |
| JP (1) | JP2009509120A (en) |
| CN (1) | CN101268326A (en) |
| WO (1) | WO2007039478A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102721262A (en) * | 2012-07-04 | 2012-10-10 | 开封空分集团有限公司 | Crude krypton and xenon extraction system and process for extracting crude krypton and xenon by utilizing same |
| CN114017992A (en) * | 2021-11-09 | 2022-02-08 | 四川空分设备(集团)有限责任公司 | Air separation system suitable for LNG cold energy load changes |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
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| EP1972875A1 (en) * | 2007-03-23 | 2008-09-24 | L'AIR LIQUIDE, S.A. pour l'étude et l'exploitation des procédés Georges Claude | Process and apparatus for the separation of air by cryogenic distillation |
| US20120174625A1 (en) * | 2009-08-11 | 2012-07-12 | Linde Aktiengesellschaft | Method and device for producing a gaseous pressurized oxygen product by cryogenic separation of air |
| EP2369281A1 (en) * | 2010-03-09 | 2011-09-28 | Linde Aktiengesellschaft | Method and device for cryogenic decomposition of air |
| US20150345859A1 (en) * | 2013-02-25 | 2015-12-03 | Mitsubishi Heavy Industries Compressor Corporation | Carbon dioxide liquefaction device |
| JP6290703B2 (en) * | 2014-05-08 | 2018-03-07 | レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード | Liquefied gas manufacturing apparatus and manufacturing method |
| EP2980514A1 (en) * | 2014-07-31 | 2016-02-03 | Linde Aktiengesellschaft | Method for the low-temperature decomposition of air and air separation plant |
| US20160245585A1 (en) * | 2015-02-24 | 2016-08-25 | Henry E. Howard | System and method for integrated air separation and liquefaction |
| EP3101374A3 (en) * | 2015-06-03 | 2017-01-18 | Linde Aktiengesellschaft | Method and installation for cryogenic decomposition of air |
| WO2019104524A1 (en) * | 2017-11-29 | 2019-06-06 | 乔治洛德方法研究和开发液化空气有限公司 | Cryogenic distillation method and apparatus for producing pressurized air by means of expander booster in linkage with nitrogen expander for braking |
| CN111527361B (en) * | 2017-12-29 | 2022-03-04 | 乔治洛德方法研究和开发液化空气有限公司 | Method and equipment for producing air product based on cryogenic rectification |
| US11054182B2 (en) * | 2018-05-31 | 2021-07-06 | Air Products And Chemicals, Inc. | Process and apparatus for separating air using a split heat exchanger |
| FR3090831B1 (en) | 2018-12-21 | 2022-06-03 | L´Air Liquide Sa Pour L’Etude Et L’Exploitation Des Procedes Georges Claude | Cryogenic distillation air separation apparatus and method |
| CN114174747B (en) * | 2019-07-26 | 2024-05-28 | 乔治洛德方法研究和开发液化空气有限公司 | Method and apparatus for separating air by cryogenic distillation |
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| US4345925A (en) * | 1980-11-26 | 1982-08-24 | Union Carbide Corporation | Process for the production of high pressure oxygen gas |
| US5379598A (en) * | 1993-08-23 | 1995-01-10 | The Boc Group, Inc. | Cryogenic rectification process and apparatus for vaporizing a pumped liquid product |
| GB9325648D0 (en) * | 1993-12-15 | 1994-02-16 | Boc Group Plc | Air separation |
| US5475980A (en) * | 1993-12-30 | 1995-12-19 | L'air Liquide, Societe Anonyme Pour L'etude L'exploitation Des Procedes Georges Claude | Process and installation for production of high pressure gaseous fluid |
| FR2721383B1 (en) * | 1994-06-20 | 1996-07-19 | Maurice Grenier | Process and installation for producing gaseous oxygen under pressure. |
| US6009723A (en) * | 1998-01-22 | 2000-01-04 | Air Products And Chemicals, Inc. | Elevated pressure air separation process with use of waste expansion for compression of a process stream |
| US5901576A (en) * | 1998-01-22 | 1999-05-11 | Air Products And Chemicals, Inc. | Single expander and a cold compressor process to produce oxygen |
| US6178775B1 (en) * | 1998-10-30 | 2001-01-30 | The Boc Group, Inc. | Method and apparatus for separating air to produce an oxygen product |
| US6112550A (en) * | 1998-12-30 | 2000-09-05 | Praxair Technology, Inc. | Cryogenic rectification system and hybrid refrigeration generation |
| ATE269526T1 (en) * | 1999-07-05 | 2004-07-15 | Linde Ag | METHOD AND DEVICE FOR THE LOW TEMPERATURE SEPARATION OF AIR |
| FR2806152B1 (en) * | 2000-03-07 | 2002-08-30 | Air Liquide | PROCESS AND INSTALLATION FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
| US6260380B1 (en) * | 2000-03-23 | 2001-07-17 | Praxair Technology, Inc. | Cryogenic air separation process for producing liquid oxygen |
| US6357258B1 (en) * | 2000-09-08 | 2002-03-19 | Praxair Technology, Inc. | Cryogenic air separation system with integrated booster and multicomponent refrigeration compression |
| US6626008B1 (en) * | 2002-12-11 | 2003-09-30 | Praxair Technology, Inc. | Cold compression cryogenic rectification system for producing low purity oxygen |
| US6962062B2 (en) * | 2003-12-10 | 2005-11-08 | L'Air Liquide, Société Anonyme à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Proédés Georges Claude | Process and apparatus for the separation of air by cryogenic distillation |
| EP1750074A1 (en) * | 2005-08-02 | 2007-02-07 | Linde Aktiengesellschaft | Process and device for the cryogenic separation of air |
-
2005
- 2005-09-23 EP EP05108826A patent/EP1767884A1/en not_active Withdrawn
-
2006
- 2006-09-21 EP EP06793721A patent/EP1938032A1/en not_active Withdrawn
- 2006-09-21 US US12/067,672 patent/US20080223075A1/en not_active Abandoned
- 2006-09-21 JP JP2008531702A patent/JP2009509120A/en active Pending
- 2006-09-21 WO PCT/EP2006/066601 patent/WO2007039478A1/en active Application Filing
- 2006-09-21 CN CNA2006800349904A patent/CN101268326A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102721262A (en) * | 2012-07-04 | 2012-10-10 | 开封空分集团有限公司 | Crude krypton and xenon extraction system and process for extracting crude krypton and xenon by utilizing same |
| CN114017992A (en) * | 2021-11-09 | 2022-02-08 | 四川空分设备(集团)有限责任公司 | Air separation system suitable for LNG cold energy load changes |
Also Published As
| Publication number | Publication date |
|---|---|
| EP1938032A1 (en) | 2008-07-02 |
| US20080223075A1 (en) | 2008-09-18 |
| JP2009509120A (en) | 2009-03-05 |
| WO2007039478A1 (en) | 2007-04-12 |
| EP1767884A1 (en) | 2007-03-28 |
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