CN100432601C - Cryogenic distillation method and installation for air separation - Google Patents

Cryogenic distillation method and installation for air separation Download PDF

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Publication number
CN100432601C
CN100432601C CNB200580002063XA CN200580002063A CN100432601C CN 100432601 C CN100432601 C CN 100432601C CN B200580002063X A CNB200580002063X A CN B200580002063XA CN 200580002063 A CN200580002063 A CN 200580002063A CN 100432601 C CN100432601 C CN 100432601C
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China
Prior art keywords
air
turbine
supercharger
pressure
exchange pipeline
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CNB200580002063XA
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Chinese (zh)
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CN1910419A (en
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P·勒博
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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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
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • 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
    • 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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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04151—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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    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • 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
    • 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
    • F25J3/0446—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the heat generated by mixing two different phases
    • 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
    • F25J3/0446—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the heat generated by mixing two different phases
    • F25J3/04466—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using the heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid oxygen
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • 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
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/52—Oxygen production with multiple purity O2
    • 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
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    • F25J2215/54—Oxygen production with multiple pressure O2
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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
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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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    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air

Abstract

The invention relates to a method and installation for separation of air by means of cryogenic distillation. According to the invention, all of the air is brought to a high pressure greater than the medium pressure and purified. Part of the purified air flow (11) is cooled in an exchange line (9) and, subsequently, divided into two fractions (13, 15). Each of the fractions expands in a turbine (17, 19), the intake pressure of the two turbines being greater than the medium pressure by at least 5 bars. Moreover, the discharge pressure of at least one of the two turbines is essentially equal to the medium pressure. At least part of the air that was expanded in at least one of the turbines is conveyed to the medium pressure column of a double or triple column. Subsequently, a cold booster (23), which is mechanically connected to one (19) of the expansion turbines, draws the air which was cooled in the main exchange line and releases said air at a temperature greater than the intake temperature. The fluid thus compressed is reintroduced into the main exchange line, in which at least one part of the fluid condenses. In addition, at least one pressurised liquid (25) originating from one of the columns (200) is vaporised in the exchange line at an evaporating temperature and the turbine (17) which is not connected to the cold booster is connected to a booster (5) followed by a cooler.

Description

Cryogenic distillation method and the equipment that is used for air separation
Technical field
The present invention relates to a kind of method and apparatus by separating air by cryogenic distillation.
Background technology
Carrying out heat exchange with the Compressed Gas that is higher than cryogenic temperature by fluid under pressure in the exchange pipeline of air separation equipment gasifies being known from the forced air process gas.From FR-A-2 688 052, EP-A-0644388, EP-A-1014020 and patent application FR 03/01722 known such equipment.
The thermal efficiency of these known devices is not very high, because the hot-fluid relevant with the low temperature compression gone into must discharge.
In addition, under situation such as the scheme shown in Figure 7 of US-A-5 475 980, the whole turbine that is connected on the low temperature supercharger is associated with energy absorber system (oil brake) on the axle that is combined in machine, and is limited in (about 70kW) under the lower power levels technically.
In any case such method is useful economically really, especially when the recycling that does not almost have energy or energy can obtain under low cost.Therefore, the technical limitations of oil brake that can overcome on the axle that is integrated in the turbine/booster assembly may be useful.
Summary of the invention
The objective of the invention is to propose a kind of replacement scheme, make it possible to realize not to be integrated in based on the low temperature supercharger process program of the energy-dissipation system on the axle of turbine/booster, design is applied to this scheme the air separation equipment of all size in practice thus.
A theme of the present invention be a kind of in the equipment that comprises double-tower type or three-tower type air separation and exchange pipeline by separating air by cryogenic distillation, work under the pressure of pressure the tower of working under elevated pressures in the described air separation is being called in, wherein:
A) with all supercharging airs to high pressure and purify, than middle pressure height at least 5bar, alternatively under this high pressure carry out alternatively by described purification for this high pressure;
B) part of purified air stream is cooled off in the exchange pipeline, is divided into two parts then;
C) each part expands in turbine;
D) press height 5bar at least in the admission pressure of described two turbines ratio;
E) discharge pressure of at least one in described two turbines is substantially equal to middle pressure;
F) at least a portion of the air that expands at least one that will be in turbine is delivered to the medium pressure column in double tower or three towers;
G) the low temperature supercharger that is mechanically connected in the expansion turbine one sucks the air that has cooled off in the exchange pipeline, and be higher than this air of conveying under the temperature of intake air temperature, and the fluid that will compress is like this introduced in the exchange pipeline again, and (vacation) condensation takes place at least a portion of fluid in the exchange pipeline;
H) from one at least a fluid under pressure in the described tower (vacation) gasification takes place under gasification temperature in the exchange pipeline,
It is characterized in that:
I) turbine that is not connected to the low temperature supercharger is connected to the supercharger that is provided with cooler thereafter; And, alternatively,
Ii) the intake air temperature of low temperature supercharger approaches liquid (vacation) gasification temperature.
According to other optional aspect of the present invention:
-described equipment also comprises mixing column except double tower or three towers, be sent to this mixing column from least one the air in the described turbine;
-deliver at least one air in the turbine of described mixing column upstream from that supercharger that is different from the low temperature supercharger, and leave this supercharger under the pressure of high pressure being higher than;
-will deliver to the bottom of mixing column so that participate in mass exchange from least one the air in the turbine; And
-the air that will be in high pressure is delivered to the bottom reboiler of mixing column, and this air is condensation at least in part in described bottom reboiler before being sent to double tower or three towers.
Another theme of the present invention is the equipment by separating air by cryogenic distillation, and this equipment comprises:
A) double-tower type or three-tower type air separation are worked under the pressure of pressing during the tower of working under elevated pressures in the described air separation is being called;
B) exchange pipeline;
C) be used for making all supercharging airs to the device that is higher than the high pressure of pressing, and the device that is used to purify this air, under this high pressure, purify alternatively;
D) be used for sending the part of purified air stream to the exchange pipeline so that cool off the device of this air stream, and be used for and cool off the device that air is divided into two parts;
E) two turbines and the device that is used for a air is delivered to each turbine;
F) at least a portion that is used for the air that will expand at least one of turbine is delivered to the device of the medium pressure column of described double tower or three towers;
G) low temperature supercharger, the air that is used for preferably extracting from the centre position of main exchange pipeline is delivered to the device of this low temperature supercharger, and the device that is used for the air of supercharging in this low temperature supercharger is sent at the place, centre position of described extraction position upstream the exchange pipeline;
H) be used for making device, be used for described at least a fluid under pressure is sent to the device of exchange pipeline from one at least a liquid pressurization of described tower, and the device that is used for going out from the exchange tubes rows gasified liquid; And
I) described low temperature supercharger is connected in the turbine one,
It is characterized in that the turbine that is not connected to described low temperature supercharger is connected to the supercharger that is provided with cooler thereafter.
According to other optional aspect, this equipment comprises:
-mixing column and be used for air is delivered to the device of described mixing column from least one of turbine;
-being used for the part of air of compressing is delivered to the device of at least one expansion turbine of mixing column upstream in supercharger, described supercharger constitutes energy dissipation unit or forms the part of energy dissipation unit;
-be used for and will send mixing column to so that participate in the device of mass exchange from least one air of turbine; And
-be used for the air that is in high pressure is sent to the device of the bottom reboiler of mixing column, and be used for this bottom reboiler at least in part the air of condensation deliver to the device of double tower or three towers.
To use with the first turbine/booster assembly concurrent working and be equipped with the additional turbine of the energy-dissipation system of oneself.Advantageously, this system is provided with the supercharger that is installed in the water cooler in dim thereafter.
Statement " pressure is approaching " is meant that pressure differs maximum 5bar, preferably maximum 2bar.Statement " temperature is approaching " is meant that temperature differs maximum 15 ℃, preferably maximum 10 ℃.
Supercharger is a single-stage compressor.
All pressure of mentioning all are absolute pressures.
Term " condensation " comprises false condensation.
Term " gasification " comprises false gasification.
The difference of the present invention and US-A-5 475 980 is, in Fig. 4 (optional turbine 9), the admission pressure of two turbines 8,32 differs greatly, difference is at least 14bar, and in Fig. 5, pressure differential is that an about 13bar and a turbine under low pressure discharge, and this production for pure oxygen is disadvantageous.
Description of drawings
Describe the present invention below with reference to accompanying drawings in detail, in the accompanying drawings:
Fig. 1 and 2 illustrates according to air separation equipment of the present invention.
The specific embodiment
In Fig. 1, the air stream under the atmospheric pressure is compressed to about 15bar in a main compressor (not shown).Then, alternatively this air was cooled off before removing impurity at this air of purification (not shown).Separated into two parts will purify air.Part of air 3 is delivered to supercharger 5, in this supercharger, air is compressed to the pressure between 17 to 20bar, then pressurized air before the warm end of the main exchange pipeline 9 that is sent to air separation equipment by water cooler 7 coolings.Pressurized air 11 was cooled to a medium temperature before leaving the exchange pipeline and being divided into two parts.Certainly, stream 11 portion can continue to cool off the cold junction until arriving exchange pipeline 9, from the discharge that is liquefied of this part of this cold junction.A 13 deliver to turbine 17, and remaining portion 15 is delivered to turbine 19.These two turbines have identical intake air temperature and pressure and identical delivery temperature and pressure, but these temperature and pressures are certainly closer to each other rather than equal.Two strands of air-flows by turbine output mix formation air stream 21, and the part 121 of this air stream is delivered to double tower, and remaining part 122 is delivered to mixing column 300.Stream 122 constitutes the part of stream 21, perhaps alternatively, is the portion that constitutes the gaseous state part of stream 21 under the situation of two phase flow at stream 21.Certainly, also can deliver to medium pressure column 100 and therefrom extract gaseous state part 122 and deliver to mixing column all flowing 21, medium pressure column have replaced phase-splitter in this case.The pressure of medium pressure column and mixing column can be different.As modification, turbine 19 can be the air blast turbine of carrying under lower pressure column pressure.
The pressure that constitutes the raw air remainder is another part 2 of the air of 15bar is cooled to the intake air temperature that is higher than turbine 17,19 in the exchange pipeline a medium temperature, in second supercharger 23, be compressed to about 30bar, and under higher temperature, introduce again in the exchange pipeline 9 so that continue cooling.
Like this, the air 37 that pressure is about 30bar liquefies in the exchange pipeline, and liquid oxygen 25 gasifies in the exchange pipeline, and the gasification temperature of this liquid is near the intake air temperature of second supercharger 23.Liquefied air leaves the exchange pipeline and is sent to Tower System.
Useless nitrogen stream 27 is heated in exchange pipeline 9.
First supercharger 5 is connected in the turbine one 17 or 19, and second supercharger 23 is connected in the turbine another on 19 or 17.
The Tower System of air separation equipment is by forming with the lower pressure column 200 hot linked medium pressure columns 100 with steeple, mixing column 300 and optional argon air tower (not shown).Lower pressure column not necessarily will have steeple.
Medium pressure column is worked under the pressure of 5.5bar, but also can be at high pressure operation more.
From the air 121 of two turbines 17,19 is the stream of sending in the bottom of medium pressure column 100.
Liquefied air 37 is in valve 39 or expand in turbine alternatively, and delivers to Tower System.
Rich solution 51, bottom lean solution 53 and top lean solution 55 in valve, expand and the sub-cooled step after deliver to lower pressure column 200 from medium pressure column 100.
Liquid oxygen is delivered to exchange pipeline 9 by pump 500 pressurizations and as fluid under pressure 25.Other liquid (no matter whether pressurizeing) can gasify in the exchange pipeline.
Alternatively, extract gaseous nitrogen and cooling exchange pipeline 9 once more from medium pressure column.
After being used for the sub-cooled withdrawing fluid, nitrogen 33 is extracted by the top from lower pressure column and heats the exchange pipeline.
After being used for the sub-cooled withdrawing fluid, useless nitrogen 27 is extracted by the lower position from lower pressure column and heats the exchange pipeline.
Alternatively, tower can be produced argon gas by the stream of handling in the suction lower pressure column 200 51.If argon air tower is arranged, stream 52 is bottom liquids of sending here from this argon air tower.
Mixing column 300 is supplied to the oxygen enriched liquid 35 that extracts and pass through pump 600 pressurizations from the centre position of lower pressure column 200 at the top, be supplied to the gaseous air stream 122 from turbine 17,19 in the bottom.Mixing column basically in depress work.
Extract gaseous oxygen air-flow 37 heating exchange pipeline 9 then from the mixing column top, after the bottom is extracted liquid stream 41 and expanded, deliver to lower pressure column in a valve.Can extract the intermediate flow that is sent to lower pressure column from tower 300.
In Fig. 2, the air stream under the atmospheric pressure is compressed to about 15bar in a main compressor (not shown).Then, alternatively this air was cooled off before removing impurity at this air of purification (not shown).Separated into two parts will purify air.Part of air 3 is delivered to supercharger 5, in this supercharger, air is compressed to the pressure between 17 to 20bar, then pressurized air before the warm end of the main exchange pipeline 9 that is sent to air separation equipment by water cooler 7 coolings.Pressurized air 11 was cooled to a medium temperature before being divided into two part 103,123.A 103 leave the exchange pipeline and are divided into two parts once more.A 13 deliver to turbine 17, and remaining portion 15 is delivered to turbine 19.These two turbines have identical intake air temperature and pressure and identical delivery temperature and pressure, but these temperature and pressures are certainly closer to each other rather than equal.Two strands of air-flows by turbine output mix formation air stream 21, and the part 121 of this air stream is delivered to double tower, and remaining part 122 is delivered to mixing column 300.As modification, turbine 19 can be the air blast turbine of carrying under lower pressure column pressure.
A 123 continue cooling in exchange pipeline 9, and discharge from the cold junction upstream and deliver to the bottom reboiler 301 of mixing column 300, in this reboiler this portion at least in part condensation to form stream 125.
The pressure that constitutes the raw air remainder is another part 2 of the air of 15bar is cooled to the intake air temperature that is higher than turbine 17,19 in the exchange pipeline a medium temperature, in second supercharger 23, be compressed to about 30bar, and under higher temperature, introduce again in the exchange pipeline 9 so that continue cooling.
Like this, the air 37 that pressure is about 30bar liquefies in the exchange pipeline, and liquid oxygen 25 gasifies in the exchange pipeline, and the gasification temperature of this liquid is near the intake air temperature of second supercharger 23.Liquefied air leaves the exchange pipeline, and be sent to Tower System after liquefied air 125 from reboiler 301 mixes.
Useless nitrogen stream 27 is heated in exchange pipeline 9.
First supercharger 5 is connected in the turbine one 17 or 19, and second supercharger 23 is connected in the turbine another on 19 or 17.
The Tower System of air separation equipment is by forming with the lower pressure column 200 hot linked medium pressure columns 100 with steeple, mixing column 300 and optional argon air tower (not shown).Lower pressure column not necessarily will have steeple.
Medium pressure column is worked under the pressure of 5.5bar, but also can be at high pressure operation more.
From the gaseous air 21 of two turbines 17,19 is the stream of sending in the bottom of medium pressure column 100.
Liquefied air 37 expands in valve 39 and delivers to medium pressure column 100 at least.
Rich solution 51, bottom lean solution 53 and top lean solution 55 in valve, expand and the sub-cooled step after deliver to lower pressure column 200 from medium pressure column 100.
Liquid oxygen is delivered to exchange pipeline 9 by pump 500 pressurizations and as fluid under pressure 25.In addition or as an alternative, other liquid (no matter whether pressurizeing) can gasify in the exchange pipeline.
Alternatively, extract gaseous nitrogen and cooling exchange pipeline 9 once more from medium pressure column.
After being used for the sub-cooled withdrawing fluid, nitrogen 33 is extracted by the top from lower pressure column and heats the exchange pipeline.
After being used for the sub-cooled withdrawing fluid, useless nitrogen 27 is extracted by the lower position from lower pressure column and heats the exchange pipeline.
Alternatively, tower can be produced argon gas by the stream of handling in the suction lower pressure column 200 51.
Mixing column 300 only is supplied to the oxygen enriched liquid 35 that extracts and pass through pump 600 pressurizations from the centre position of lower pressure column 200 at the top.Mixing column basically in depress work.By changing the pressure of stream 123, work under the pressure that mixing column 300 can be pressed in being different from.Alternatively, the part of rich solution 51 can be delivered to the bottom of tower 300.
Extract gaseous oxygen air-flow 37 and heating exchange pipeline 9 from the mixing column top, after the bottom is extracted liquid stream 41 and expanded, deliver to lower pressure column in a valve.

Claims (14)

1. one kind is comprising double-tower type or three-tower type air separation (100,200) method by separating air by cryogenic distillation and in the equipment of exchange pipeline (9), work under the pressure of pressing during the tower of working under elevated pressures in the described air separation (100) is being called, wherein:
A) with all supercharging airs to high pressure and purify;
B) part of purified air stream is cooled off in the exchange pipeline, is divided into two parts then;
C) each part is expanded in one in two turbines (17,19) respectively;
D) press height 5bar at least in the admission pressure of described two turbines ratio;
E) discharge pressure of at least one in described two turbines is substantially equal to middle pressure;
F) at least a portion of the air that expands at least one that will be in turbine is delivered to the medium pressure column in double tower or three towers;
G) the low temperature supercharger (23) that is mechanically connected in the turbine one sucks the air that has cooled off in the exchange pipeline, and be higher than this air of conveying under the temperature of intake air temperature, and the fluid that will compress is like this introduced in the exchange pipeline again, at least a portion generation condensation of fluid in the exchange pipeline;
H) from one at least a fluid under pressure in the described air separation the exchange pipeline under gasification temperature generating gasification, and,
I) turbine (17) that is not connected to the low temperature supercharger is connected to the supercharger (5) that is provided with cooler thereafter,
It is characterized in that described equipment also comprises mixing column (300) except double tower or three towers, and be sent to this mixing column from least one the air in the described turbine (17,19).
2. the method for claim 1, it is characterized in that, deliver at least one air in the turbine (17,19) of described mixing column upstream from that supercharger (5) that is different from low temperature supercharger (23), and leave this supercharger under the pressure of high pressure being higher than.
3. method as claimed in claim 1 or 2 is characterized in that, the air (13,15) that expands at least one in turbine (17,19) is sent to the bottom of mixing column (300) so that participate in the mass exchange at this place.
4. the method for claim 1 is characterized in that, the air (123) that is in high pressure is at least delivered to the bottom reboiler (301) of mixing column (300), and this air is condensation at least in part in described bottom reboiler before being sent to double tower or three towers.
5. the method for claim 1 is characterized in that, presses height 5bar at least in the described high pressure ratio.
6. method as claimed in claim 5 is characterized in that described purification is carried out under described high pressure.
7. the method for claim 1 is characterized in that, the intake air temperature of described low temperature supercharger (23) approaches the gasification temperature of liquid.
8. the method for claim 1 is characterized in that, from the described turbine (17,19) at least one air through medium pressure column (100) be sent to described mixing column afterwards.
9. equipment by separating air by cryogenic distillation comprises:
A) double-tower type or three-tower type air separation (100,200) are worked under the pressure of pressing during the tower of working under elevated pressures in the described air separation (100) is being called;
B) exchange pipeline (9);
C) be used for making all supercharging airs to the device that is higher than the high pressure of pressing, and the device that is used to purify this air;
D) be used for sending the part of purified air stream to the exchange pipeline so that cool off the device of this air stream, and be used for and cool off the device that air is divided into two parts;
E) two turbines (17,19) and the device that is used for a air is delivered to each turbine;
F) at least a portion that is used for the air that will expand at least one of turbine is delivered to the device of the medium pressure column of described double tower or three towers;
G) low temperature supercharger (23), be used for extracting the air that extracts the position and deliver to the device of this low temperature supercharger from one of exchange pipeline, and the device that is used for the air of supercharging in this low temperature supercharger is sent at the place, centre position of described extraction position upstream the exchange pipeline;
H) be used for making device (500), be used for pressurized liquid is sent to the device of exchange pipeline from one at least a liquid pressurization of described air separation, and the device that is used for going out from the exchange tubes rows gasified liquid;
I) described low temperature supercharger is connected to (19) in the turbine; And
J) turbine (17) that is not connected to described low temperature supercharger is connected to the supercharger (5) that is provided with cooler thereafter,
It is characterized in that this equipment comprises mixing column and is used at least one from turbine (17,19) of air delivered to the device of described mixing column.
10. equipment as claimed in claim 9, it is characterized in that, this equipment comprises at least one turbine (17 that is used for the part of air of compression in the supercharger that is provided with cooler thereafter (5) is delivered to the mixing column upstream, 19) device, the described supercharger (5) that is provided with cooler thereafter constitute energy dissipation unit or form the part of energy dissipation unit.
11., it is characterized in that this equipment comprises and is used for and will sends mixing column to so that participate in the device of the mass exchange at this place from least one the air in the turbine (17,19) as claim 9 or 10 described equipment.
12. equipment as claimed in claim 9, it is characterized in that, this equipment comprises that the air (123) that is used for being in high pressure at least sends the device of the bottom reboiler (301) of mixing column (300) to, and be used for this bottom reboiler at least in part the air of condensation deliver to the device of double tower or three towers.
13. equipment as claimed in claim 9 is characterized in that, the described device that is used to purify air purifies under described high pressure.
14. equipment as claimed in claim 9 is characterized in that, described extraction position is positioned at the centre position of exchange pipeline.
CNB200580002063XA 2004-01-12 2005-01-07 Cryogenic distillation method and installation for air separation Expired - Fee Related CN100432601C (en)

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