CN1737476A - Method and device for obtaining gaseous pressure product by hypothermia air separation - Google Patents
Method and device for obtaining gaseous pressure product by hypothermia air separation Download PDFInfo
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- CN1737476A CN1737476A CNA200510091800XA CN200510091800A CN1737476A CN 1737476 A CN1737476 A CN 1737476A CN A200510091800X A CNA200510091800X A CN A200510091800XA CN 200510091800 A CN200510091800 A CN 200510091800A CN 1737476 A CN1737476 A CN 1737476A
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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
- F25J3/04103—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 using solely hydrostatic liquid head
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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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
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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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
- F25J3/04818—Start-up of the process
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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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
- F25J3/04824—Stopping of the process, e.g. defrosting or deriming; Back-up procedures
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
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- 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/62—Details of storing a fluid in a tank
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
A process and system are used for obtaining a gaseous pressure product by cryogenic separation of air. In the normal operation, charge air is condensed, cooled and fed to a distillation column system (1); a product fraction is withdrawn-in a liquid condition from the distillation column system, and is introduced into a liquid tank; product liquid is removed from the liquid tank, is pressurized in a pump set (6) in the liquid condition to an increased pressure, is evaporated in an indirect heat exchange with a first heat transfer medium flow, and is withdrawn as a gaseous pressure product. In an emergency operation, product liquid is removed from the liquid tank, is brought in the liquid condition to an increased pressure (6), is evaporated in an indirect heat exchange (62) with a second heat transfer medium flow, and is withdrawn as a gaseous pressure product (63). In a bypass operation, the product fraction (2) withdrawn in the liquid condition from the distillation column system is guided past the liquid tank (70); is brought via the pump set (6) in the liquid condition to an increased pressure; is evaporated in an indirect heat exchange (8), and is withdrawn as a gaseous pressure product (9).
Description
Technical field
The present invention relates to a kind of method of obtaining the pressure product of gaseous state by Cryogenic air separation.
The invention still further relates to a kind of equipment that obtains the pressure product of gaseous state by cryogenic air separation.
Background technology
The method and apparatus of cryogenic air separation (air separation) is open by the cryogenic technique (second edition in 1985, the 4th chapter, the 281st page to 337 pages) of Hausen/Linde.Distillation column system of the present invention can be configured for single Tower System that nitrogen-oxygen separates, and also can be configured to double tower system (for example Jing Dian woods moral double tower system), perhaps also can be configured to three towers or multitower system.Except these posts that are used for nitrogen-oxygen separation, can also have some other and be used to obtain for example equipment of argon of some other constituent of air, especially inert gas.
Method of the present invention belongs to the category of interior compression (Innenverdichtung) process.At this, normally in service, the product of distillation column system at least a (for example from the single tower of single Tower System, from the high-pressure tower of double tower or three-tower system and/or from the nitrogen of the MDS tower of three-tower system, perhaps alternatively or additionally, from the single tower of single Tower System, from the MDS tower of three-tower system and/or from the oxygen of the lower pressure column of double tower or three-tower system) with liquid form by among of these towers of three-tower system or by one with these towers in a condenser that is connected in take out, be issued to a pressure that increases in liquid state, evaporation or accurate evaporation (under the supercritical pressure) indirectly with the heat exchange of first heat-carrying agent stream time, the pressure product as gaseous state is acquired at last.First heat-carrying agent constitutes by feeding air and/or nitrogen usually.Indirect heat exchanger can be in an independent heat exchanger or is carried out in a main heat exchanger that also carries out the feeding air cooling therein.
Compression method is for example open by following document in this: DE 830805, DE 901542 (=US 2712738/US 2784572), DE 952908, DE 1103363 (=US3083544), DE 1112997 (=US 3214925), DE 1124529, DE 1117616 (=US3280574), DE 1226616 (=US 3216206), DE 1229561 (=US 3222878), DE 1199293, DE 1187248 (=US 3371496), DE 1235347, DE 1258882 (=US 3426543), DE 1263037 (=US 3401531), DE 1501722 (=US3416323), DE 1501723 (=US 3500651), DE 2535132 (=US 4279631), DE 2646690, EP 93448B1 (=US 4555256), EP 384483B1 (=US5036672), EP 505812B1 (=US 5263328), EP 716280B1 (=US5644934), EP 842385B1 (=US 5953937), EP 758733B1 (=US5845517), EP 895045B1 (=US 6038885), DE 19803437A1, EP 949471B1 (=US 6185960B1), EP 955509A1 (=US 6196022B1), EP 1031804A1 (=US 6314755), DE 19909744A1, EP 1067345A1 (=US 6336345), EP 1074805A1 (=US 6332337), DE 19954593A1, EP 1134525A1 (=US6477860), DE 10013073A1, EP 1139046A1, EP 1146301A1, EP1150082A1, EP 1213552A1, DE 10115258A1, EP 1284404A1 (=US2003051504A1), EP 1308680A1 (=US 6612129B2), DE 10213212A1, DE 10213211A1, EP 1357342A1 or DE 10238282A1.
Pressure in the liquid improves and can be undertaken by any known method, for example by pump, utilize static pressure potential energy (hydrostatischen Potentials) and/or pressurization evaporation (Druckaufbauverdampfung) in jar.
" evaporation " this notion comprises standard evaporation under the supercritical pressure at this.Therefore the pressure that reaches of product liquid also can be higher than critical pressure, as with nitrogen upstream by the pressure of the heat-carrying agent of (standard) condensation.
Open by EP 895045B1 (=US 6038885), the device that liquid tank and the pressure that is used for liquid tank then improve both can be used for interior compression, also can be used for emergency operating, emergency operating allows to continue to provide the pressure product of gaseous state under the situation of distillation column system fault.In emergency operating, the product liquid that reaches pressure relatively another, the second heat-carrying agent stream is evaporated, normally in an atmospheric evaporation device or a water-bath evaporimeter, be evaporated.This combination has many advantages.Yet, in case need maintain or repair liquid tank the time, must disconnect by whole equipment, no matter be normally move or emergency operating under.
Summary of the invention
Task of the present invention is, further improves the availability of said system.
According to the present invention, proposed a kind ofly to obtain the method for the pressure product of gaseous state by Cryogenic air separation,
Wherein, when normal operation:
-feeding air is compressed, cools off and be transported to a distillation column system,
-by taking out a kind of product cut in the distillation column system and import in the liquid tank liquidly,
-from liquid tank, take out product liquid, this product liquid is issued to the pressure of a raising in liquid state in the pump group of a single pump with one or more parallel connections, with the indirect heat exchange of first heat-carrying agent stream in evaporation and be removed as the pressure product of gaseous state;
Wherein, when emergency operating:
-from liquid tank, take out product liquid, this product liquid is issued to the pressure of a raising in liquid state, with the indirect heat exchange of second heat-carrying agent stream in evaporation and be removed as the pressure product of gaseous state;
Wherein, in service a bypass:
-the product cut that takes out from distillation column system is walked around liquid tank with being in a liquid state, is issued to the pressure of a raising in the pump group in liquid state, evaporation and be removed as the pressure product of gaseous state in indirect heat exchange.
According to the present invention, a kind of equipment that obtains the pressure product of gaseous state by cryogenic air separation has also been proposed, it has: a distillation column system, a liquid tank, a adjusting device with the pump group of the single pump of one or more parallel connections, a main heat exchanger and an emergent heat exchanger, a conditioning equipment operation in normal operation and emergency operating, wherein:
Normally in service:
-feeding air is compressed, cools off and be transported to distillation column system,
-take out product cut with being in a liquid state and import to the liquid tank from distillation column system,
-product liquid is removed from liquid tank, is issued to the pressure of a raising in the pump group in liquid state, in main heat exchanger with the indirect heat exchange of first heat-carrying agent stream in evaporation and be removed as the pressure product of gaseous state;
In emergency operating:
-product liquid is removed from liquid tank, is issued to the pressure of a raising in the pump group in liquid state, with the indirect heat exchange of second heat-carrying agent stream in evaporation and be removed in emergent heat exchanger as the pressure product of gaseous state;
Wherein, in addition, adjusting device is in the operation of bypass such conditioning equipment in service, that is, in service in bypass:
-the product cut that takes out from distillation column system is walked around liquid tank with being in a liquid state, is issued to the pressure of a raising in liquid state, evaporation and be removed as the pressure product of gaseous state in indirect heat exchange.
This task is to solve like this.One the 3rd running status is set in the method for the invention, i.e. bypass operation.At this moment, walk around liquid tank with being in a liquid state, in the pump group, be issued to the pressure of a raising, when carrying out heat exchange with the first heat-carrying agent stream indirectly, evaporate, and be removed as the pressure product of gaseous state in liquid state by the product cut that takes out in the distillation column system.Improve for pressure and evaporation can be provided with independent device in principle at this.Use and normal identical device (as pump and heat exchanger) in service and identical heat-carrying agent stream but usually advantageously, bypass is in service for this reason.
Within the scope of the invention, be compressed in this in jar time that can not be used and still can proceed.This equipment can continue to provide the pressure product of gaseous state.Also can utilize the bypass operation but have in purity under the situation of temporary transient fluctuation, to avoid being stored in the pollution of the product in the liquid tank from the product cut of the liquid state of distillation column system; Favourable in the case also is, walks around this liquid tank in mode according to the present invention.
The device that is used for the pressure raising under liquid state is made up of some pumps mostly.Can use a unique pump in principle.But consider that for made allowance also often using the pump group is a plurality of parallels connection of pumps.In the case, a pump group can be general two or three pumps that respectively have 50% rated power; Under the situation with three (or more) pumps, a pump only remains on dormant state (Standby), so that the task of this pump is born in an operation in other pump when breaking down.
Irrelevant with the number of pump, pump duty is generally regulated by the pump bypass of each single pump, and the unnecessary amount of the liquid that is pumped is also led again by this pump by-pass reducing and got back in the liquid tank.
Normally in service, in the pump group of a single pump with one or more parallel connections, carrying out pressure under liquid state improves, wherein at least one single pump has one first pump bypass, is at least temporarily reduced pressure by this first pump bypass and is drawn and get back in the liquid tank by the part of the product liquid of discharging in the pump; Same pump group improves at the bypass pressure that also can be used under the liquid state in service.For this situation advantageously at this, at least one single pump also has one second pump bypass except that the first pump bypass, part by the product liquid of discharging in the pump at least temporarily reduces pressure by this second pump bypass, walks around liquid tank and leads the inlet of getting back to the pump group.A plurality of pumps of preferred pump group or all pumps respectively have first and second pump bypass of above-mentioned meaning.
The present invention also can be used for the multi beam distillation column system, and they have a public liquid tank, as undocumented German patent application 102004006283 with and relevant application described in.Be introduced into liquid tank from two bundles (Straengen) of distillation column system or the product cut of a plurality of bundles this moment.No matter be liquid tank or being used for device that pressure improves jointly uses by two bundles or a plurality of bundle of distillation column system.
Description of drawings
Describe the present invention and details of the present invention in detail by an embodiment who schematically shows in the accompanying drawings below.
The specific embodiment
Take out product cut 2 from air separation unit 1 with distillation column system with being in a liquid state.In this embodiment, this distillation column system is constructed with the double tower system of high-pressure tower and lower pressure column.Oxygen from the liquid state of the pond groove of lower pressure column constitutes product cut 2.
Normally in service, liquid oxygen 2 is transported to liquid tank 4 by a valve of opening 51 through pipeline 3.Simultaneously by taking out liquid oxygen 5 (valve 52 is also opened) in the liquid tank and being transported to one by single pump or the pump group 6 formed by the single pump of a plurality of parallel connections.There, this liquid reaches approximately desired product pressure and is delivered to first evaporimeter 8 by pipeline 7 (valve 53 opens wide), flows adverse current and is evaporated at this and first heat-carrying agent.The heat-carrying agent stream preferably stream of the corresponding highland compression of the feeding air by being used for air separation unit 1 constitutes, perhaps by the elevated pressure nitrogen structure from air separation unit 1.In this embodiment, evaporimeter 8 constitutes by the main heat exchanger of air separation unit 1, and feeding air is cooled to rectification temperature in this main heat exchanger.Scheme as an alternative, evaporimeter also can be configured to the heat exchanger that separates with main heat exchanger, for example are configured to secondary condenser.Oxygen is discharged by pipeline 9 as the pressure product of gaseous state and can be drawn towards user or distribution system.
If air separation unit 1 since outage plan or unplanned and malfunctioning, system just is transformed into emergency operating.For this reason, valve 51 and 53 cuts out, and valve 61 is opened.Thus, the oxygen of the liquid state that stores in liquid tank 4 can flow to second evaporimeter 62 by pipeline 60.This second evaporimeter evaporates by " second heat-carrying agent stream ", and this second heat-carrying agent stream is different with first heat-carrying agent stream.This second evaporimeter for example is configured to atmospheric evaporation device or water-bath evaporimeter.In emergency operating, oxygen is drawn towards user or distribution system as the pressure product of gaseous state by pipeline 63.
If air separation unit 1 is in operation, but liquid oxygen 2 can not or do not wish to be imported in the liquid tank 4, then takes bypass to move.This moment, valve 51,52,54 and 61 cut out, and liquid product stream 2 is walked around liquid tank 4 by bypass duct 70 (under the situation that valve 71 is opened) and is conducted to pump group 6.
At this moment, not by above-mentioned pump bypass 10 but carry out pump by the second pump bypass 75 that has choke valve 74 and regulate that liquid can turn back in the air separation unit 1 by this second pump bypass.
As the alternative of regulating by bypass, pump is adjusted under the various ruuning situations and also can realizes by rotational speed regulation.
Claims (4)
1. obtain the method for the pressure product of gaseous state by Cryogenic air separation,
Wherein, when normal operation:
-feeding air is compressed, cools off and be transported to a distillation column system (1),
-also import (3) in liquid tank (4) by take out a kind of product cut (2) in the distillation column system (1) liquidly,
-taking-up product liquid (5) from liquid tank (4), this product liquid is issued to the pressure of a raising in liquid state in the pump group (6) of a single pump with one or more parallel connections, with the indirect heat exchange (8) of first heat-carrying agent stream in evaporate and be removed as the pressure product (9) of gaseous state;
Wherein, when emergency operating:
-from liquid tank (4), take out product liquid (5), this product liquid is issued to the pressure of (6) raisings in liquid state, with the indirect heat exchange (62) of second heat-carrying agent stream in evaporate and be removed as the pressure product (63) of gaseous state;
It is characterized in that:
It is in service a bypass,
-the product cut (2) that takes out from distillation column system (1) is walked around (70) liquid tank with being in a liquid state, is issued to the pressure of (6) raisings in pump group (6) in liquid state, evaporates in indirect heat exchange (8) and is removed as the pressure product (9) of gaseous state.
2. according to the method for claim 1, it is characterized in that: at least one single pump of pump group (6) has one first pump bypass (10), and the part of the product liquid of being discharged by pump is drawn by this at least temporarily step-down of first pump bypass (54) and quilt when normal operation gets back in the liquid tank (4); At least one single pump also has one second pump bypass (75) except the first pump bypass (10), the part of the product liquid of being discharged by pump (6) by this at least temporarily step-down of second pump bypass, is walked around liquid tank and quilt and is led and get back in the distillation column system when bypass move.
3. according to the method for claim 1 or 2, it is characterized in that: distillation column system is configured to two-beam or multi beam, wherein is introduced in the liquid tank from two bundles of distillation column system or the product cut of a plurality of bundles.
4. obtain the equipment of the pressure product of gaseous state by cryogenic air separation, it has: a distillation column system (1), a liquid tank (4), one have pump group (6), a main heat exchanger (8) and an emergent heat exchanger (62) of the single pump of one or more parallel connections, the adjusting device of a conditioning equipment operation in normal operation and emergency operating, wherein:
Normally in service:
-feeding air is compressed, cools off and be transported to distillation column system (1),
-take out (2) product cut with being in a liquid state and import (3) to liquid tank (4) from distillation column system (1),
-product liquid (5) is removed from liquid tank (4), in pump group (6), be issued to the pressure of (6) raisings in liquid state, in main heat exchanger (8) with the indirect heat exchange (8) of first heat-carrying agent stream in evaporation and be removed as the pressure product (9) of gaseous state;
In emergency operating:
-product liquid (5) is removed from liquid tank (4), in pump group (6), be issued to the pressure of (6) raisings in liquid state, with the indirect heat exchange (62) of second heat-carrying agent stream in emergent heat exchanger (62), evaporate and be removed as the pressure product (63) of gaseous state;
It is characterized in that: in addition, adjusting device is in the operation of bypass such conditioning equipment in service, that is, in service in bypass:
-the product cut (2) that takes out from distillation column system (1) is walked around (70) liquid tank with being in a liquid state, is issued to the pressure of (6) raisings in liquid state, evaporates in indirect heat exchange (8) and is removed as the pressure product (9) of gaseous state.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102004039839 | 2004-08-17 | ||
| DE102004039839.9 | 2004-08-17 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1737476A true CN1737476A (en) | 2006-02-22 |
Family
ID=35768639
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA200510091800XA Pending CN1737476A (en) | 2004-08-17 | 2005-08-17 | Method and device for obtaining gaseous pressure product by hypothermia air separation |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US20060037357A1 (en) |
| CN (1) | CN1737476A (en) |
| CA (1) | CA2515980A1 (en) |
| DE (1) | DE102005029274A1 (en) |
| FR (1) | FR2874423A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105705892A (en) * | 2013-09-10 | 2016-06-22 | 乔治洛德方法研究和开发液化空气有限公司 | Method and apparatus for separation of a gaseous mixture at sub-ambient temperature |
| CN105705884A (en) * | 2013-09-10 | 2016-06-22 | 乔治洛德方法研究和开发液化空气有限公司 | Method and device for separation at cryogenic temperature |
Families Citing this family (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102009034979A1 (en) | 2009-04-28 | 2010-11-04 | Linde Aktiengesellschaft | Method for producing pressurized oxygen by evaporating liquid oxygen using a copper and nickel heat exchanger block |
| EP2312248A1 (en) | 2009-10-07 | 2011-04-20 | Linde Aktiengesellschaft | Method and device for obtaining pressurised oxygen and krypton/xenon |
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| DE102010052544A1 (en) | 2010-11-25 | 2012-05-31 | Linde Ag | Process for obtaining a gaseous product by cryogenic separation of air |
| DE102010052545A1 (en) | 2010-11-25 | 2012-05-31 | Linde Aktiengesellschaft | Method and apparatus for recovering a gaseous product by cryogenic separation of air |
| EP2520886A1 (en) | 2011-05-05 | 2012-11-07 | Linde AG | Method and device for creating gaseous oxygen pressurised product by the cryogenic decomposition of air |
| DE102011112909A1 (en) | 2011-09-08 | 2013-03-14 | Linde Aktiengesellschaft | Process and apparatus for recovering steel |
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| DE102011121314A1 (en) | 2011-12-16 | 2013-06-20 | Linde Aktiengesellschaft | Method for producing gaseous oxygen product in main heat exchanger system in distillation column system, involves providing turbines, where one of turbines drives compressor, and other turbine drives generator |
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| WO2014154339A2 (en) | 2013-03-26 | 2014-10-02 | Linde Aktiengesellschaft | Method for air separation and air separation plant |
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| EP2963367A1 (en) | 2014-07-05 | 2016-01-06 | Linde Aktiengesellschaft | Method and device for cryogenic air separation with variable power consumption |
| EP2963370B1 (en) | 2014-07-05 | 2018-06-13 | Linde Aktiengesellschaft | Method and device for the cryogenic decomposition of air |
| EP2963369B1 (en) | 2014-07-05 | 2018-05-02 | Linde Aktiengesellschaft | Method and device for the cryogenic decomposition of air |
| TR201808162T4 (en) | 2014-07-05 | 2018-07-23 | Linde Ag | Method and apparatus for recovering a pressurized gas product by decomposing air at low temperature. |
| FR3033395A1 (en) * | 2015-03-05 | 2016-09-09 | Air Liquide | METHOD AND APPARATUS FOR COMPRESSING GAS |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3668078A (en) * | 1969-04-25 | 1972-06-06 | Phillips Petroleum Co | Fractional distillation bypass control process |
| FR2706195B1 (en) * | 1993-06-07 | 1995-07-28 | Air Liquide | Method and unit for supplying pressurized gas to an installation consuming an air component. |
| DE19732887A1 (en) * | 1997-07-30 | 1999-02-04 | Linde Ag | Air separation process |
| US7409835B2 (en) * | 2004-07-14 | 2008-08-12 | Air Liquide Process & Construction, Inc. | Backup system and method for production of pressurized gas |
-
2005
- 2005-06-23 DE DE102005029274A patent/DE102005029274A1/en not_active Withdrawn
- 2005-08-12 CA CA002515980A patent/CA2515980A1/en not_active Abandoned
- 2005-08-16 FR FR0552514A patent/FR2874423A1/en not_active Withdrawn
- 2005-08-17 CN CNA200510091800XA patent/CN1737476A/en active Pending
- 2005-08-17 US US11/205,035 patent/US20060037357A1/en not_active Abandoned
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105705892A (en) * | 2013-09-10 | 2016-06-22 | 乔治洛德方法研究和开发液化空气有限公司 | Method and apparatus for separation of a gaseous mixture at sub-ambient temperature |
| CN105705884A (en) * | 2013-09-10 | 2016-06-22 | 乔治洛德方法研究和开发液化空气有限公司 | Method and device for separation at cryogenic temperature |
| CN105705884B (en) * | 2013-09-10 | 2019-03-29 | 乔治洛德方法研究和开发液化空气有限公司 | Method and apparatus for separating at low temperature |
Also Published As
| Publication number | Publication date |
|---|---|
| DE102005029274A1 (en) | 2006-02-23 |
| FR2874423A1 (en) | 2006-02-24 |
| CA2515980A1 (en) | 2006-02-17 |
| US20060037357A1 (en) | 2006-02-23 |
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