CN105264317A - Retrofittable device for low-temperature separation of air, retrofitting system, and method for retrofitting a low-temperature air separation system - Google Patents
Retrofittable device for low-temperature separation of air, retrofitting system, and method for retrofitting a low-temperature air separation system Download PDFInfo
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- CN105264317A CN105264317A CN201480022093.6A CN201480022093A CN105264317A CN 105264317 A CN105264317 A CN 105264317A CN 201480022093 A CN201480022093 A CN 201480022093A CN 105264317 A CN105264317 A CN 105264317A
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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
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
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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
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/0469—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser and an intermediate re-boiler/condenser
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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
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/04703—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser being arranged in more than one vessel
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
- F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
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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
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
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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
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
- F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/0489—Modularity and arrangement of parts of the air fractionation unit, in particular of the cold box, e.g. pre-fabrication, assembling and erection, dimensions, horizontal layout "plot"
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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
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04969—Retrofitting or revamping of an existing air fractionation unit
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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
- F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
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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
- F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon
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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
The retrofittable device for low-temperature separation of air comprises a distillation column system, which has a high-pressure column (3), a low-pressure column (4), and a first raw argon column (6). Said device comprises supply lines (101, 102) for connecting the first raw argon column (6) to a second raw argon column (41), wherein the supply lines pass through the outer wall of the first cold box (1), which encloses the high-pressure column (3), the low-pressure column (4), and the first raw argon column (6). The invention further relates to a retrofitting system, which comprises a second cold box (40), a second raw argon column (41), and corresponding supply lines (201 to 205), and to a method for retrofitting the device mentioned first.
Description
The present invention relates to a kind of method of preamble according to claim 1.
" supply air line " and " liquid back pipe road " is the term in argon ions.Their respective independently pipelines may also be shared pipeline.In the latter case, corresponding pipeline must have relatively large cross section and the gas flow on rightabout and liquid stream are not hindered each other, and makes it possible to the function simultaneously meeting supply air line and liquid back pipe road.
" ice chest " can be regarded as insulated case herein, and it comprises completely and the heat-insulating inside of outer wall; Treat that insulation system parts are arranged on inside, such as one or more knockout tower and/or heat exchanger.By forming outer wall in the corresponding way and/or can insulation effect being brought by the space fill insulant between system unit and outer wall.When in the end different, preferably adopt pulverulent material, such as perlite.For the distillation column system of separating nitrogen and oxygen in Cryognic air separation system and main heat exchanger, and other part of cooling system must be closed by one or more ice chest.The external dimensions of ice chest determines the transportation clearance of packaging usually when prefabrication system.
Method and apparatus for Cryogenic air separation is known, such as, Hausen/Linde, Tieftemperaturtechnik [Low-temperaturetechnology], 1958 the 2nd edition, chapter 4 (281 to 337 pages).Distillation column system can be used as two Tower Systems (such as typical woods moral double tower system (Lindedoublecolumnsystem)) or is used for being separated of nitrogen and oxygen as three towers or multitower system.
If do not need to produce for low temperature argon, about the system (for energy efficiency after optimization) for reclaiming nitrogen and/or oxygen, preferred so-called imitative argon column (" the first crude argon column "), such as, described in EP540900A1.Described imitative argon column provides about 25 theoretical trays and does not produce vendible argon product, but produces the residual gas being rich in argon, and described residual gas is such as made up of 86% argon, 12% oxygen and 2% nitrogen.The residual gas being rich in argon produces the oxygen yield that improve described system.
If this system is furnished with argon production equipment by transformation subsequently, such as, especially for the production of the equipment of straight argon, shown in EP1103772A1, up to now, known method and apparatus relates to high-caliber expense.
Therefore, target of the present invention is to provide a kind of device, and it can be furnished with argon production equipment and without the need to bearing the excess overhead in reconstruct by transformation, and is also provided for the correlation method transformed and the modernization system needing relative few expense on equipment.
Described target is realized by whole features of claim 1.
Underlying inventive comprises equipment device, it is furnished with full argon production equipment (or being at least furnished with full crude argon column) by transformation and is not opened ice chest (multiple ice chest) to make energy, and the first crude argon column simultaneously existed can be reused by the Part I carrying out argon oxygen separating subsequently in the first crude argon column, and the remainder of argon oxygen separating that (only) carries out in the second crude argon column will be transformed.The corresponding outer wall through ice chest is provided and there is " the preparation pipeline " of jockey as flange for this object.When (going back) is not in normal mode by the device transformed, " preparation pipeline " keeps operating, and have corresponding occluding device in this case, it is suitable for being opened during transformation process.
The instruction of this and above-mentioned EP1103772A1 has sizable difference.Especially, with regard to above-mentioned restriction, this does not disclose any " preparation pipeline " between the first and second crude argon columns, and the tradition only disclosed between crude argon column two parts separately connects, and these two parts are not by any ice chest wall.About transforming air-seperation system, without the need to the crude argon column by means of other argon module, this openly will as any pipeline of " preparation pipeline " with regard to above-mentioned restriction equally.Even then, those skilled in the art can not infer from this pipeline realized as " preparation pipeline " between the first and second crude argon columns.
After connecting line is connected and makes transformation, it can operate the first and second crude argon columns as the distillation fraction be connected in series, and this means two parts as single distillation column, one of them is arranged on another, or one is arranged under the other.
In principle, this can realize by two kinds of different modes, that is:
-the first distortion: the first crude argon column the second crude argon column " below ",
-the second distortion: the first crude argon column the second crude argon column " above ".
Here " below " mentioned and " above " are not the spatial placement of tower but its process circuit.With regard to described process, the first tower be positioned at during the operation of system the second tower " below ", the overhead vapours of the first tower is introduced into the sump region of the second tower, and on the contrary, the sump liquid of the second tower flow to the tower top of the first tower.With regard to described process, the first tower be positioned at during Dynamic System the second tower " above ", the overhead vapours of the second tower is introduced into the sump region of the first tower, and on the contrary, the sump liquid of the first tower flow to the tower top of the second tower.
First distortion of the present invention describes in claim 2.The advantage that it has is, it uses the preparation pipeline practical function of lesser amt.
When the described distortion of transforming, in general, the first crude argon overhead condenser is closed, and is replaced by the second crude argon overhead condenser, and described second crude argon overhead condenser is to be rebuilt at the tower top of the second crude argon column to be rebuilt.
As substituting this, the first crude argon overhead condenser can continue operation after transformation, and it can be used as central evaporator.
In this case, when another preparation pipeline be provided for make to be entered the zone line of lower pressure column by the cooling fluid (in the second crude argon overhead condenser) evaporated time, it is favourable.In addition, other preparation pipeline can be provided for and will do not introduced the zone line of lower pressure column and/or the zone line for the residual gas from pure argon column being introduced lower pressure column by the cooling fluid (in the second crude argon overhead condenser) evaporated.
Claim 4 describes the second distortion of the present invention.In this connection, the first crude argon overhead condenser is possible in transformation rear continuation operation.In any case do not need transformation second crude argon overhead condenser here or only transform relative fraction.In any case only produce the adverse current being used for the first and second crude argon columns after transformation or be used for major part by the first crude argon overhead condenser, it continued to operate in the same manner before transformation in principle.
In order to connect pure argon column and pure argon column overhead condenser when transforming, preparation pipeline in addition may be provided in the framework of the second distortion, as claim 5 describes in detail.As substituting this, when the first distortion, when the second crude argon column comprises the theoretical tray of respective numbers, and the outlet of argon end product is when being arranged on the theoretical or actual plate of some under the tower top (or overhead condenser) of the second crude argon column, argon end product also directly can reclaim from the second crude argon column, as described in US5235816 for single part crude argon column; When the second distortion, described feature realizes with the corresponding manner at the first crude argon column.
In principle, the feature in conjunction with two distortion of device for modifying is also possible.Then two that transform substitute is possible.Then can make a choice while transformation.
The present invention relates in addition according to the modernization system (main system) for transforming the above-mentioned type device described in claim 6 to 9.Its connecting line is preferably arranged so that they terminate in the eminence of the connector of preparation pipeline.Under the best circumstances, the ice chest (multiple ice chest) that the ice chest of modernization system only must be close to main system is settled, and corresponding connector directly connects and connects each other each other or by short tube.
3rd, the present invention relates to a kind of method for transforming the Cryognic air separation system not having argon reclaimer according to claim 10.
When main system is not designed to have transformation ability or be not designed to have Overall Reconstruction ability, above-mentioned modernization system and the method for transforming also can be adopted.In this case, main system must adapt to from inside naturally.However, if its size allows, what modernization system can overallly be pre-installed is provided in ice chest.
The exemplary schematically shown by accompanying drawing is explained by the present invention and more details of the present invention hereinafter in more detail, wherein:
Fig. 1 illustrates the exemplary of the first distortion of the present invention, and
Fig. 2 illustrates the exemplary of the second distortion of the present invention.
What below first described by Fig. 1 is main system, does not have the Cryognic air separation system that argon reclaims, the distillation column system held in single ice chest 1 in this example.As substituting this, the tower of described distillation column system and condenser also can be arranged in two or more ice chests separated from one another.
Compression, the pre-cold-peace of operation air are filtered, the refrigeration expanded by the production work producing one or more strands of process flow, and the cooling operating air in main heat exchanger is all not shown.Main heat exchanger with distillation column system return flow indirect heat exchange time for cooling down operation air.It can be formed from single or multiple parallel connection and/or the heat exchanger sections be connected in series, such as, from one or more heat-exchangers of the plate type block.Main heat exchanger can be contained in the identical ice chest 1 with distillation column system or in independent ice chest.
First, gaseous state operation air stream 2 is introduced into the sump region of high-pressure tower 3.This is a part for distillation column system, and it comprises lower pressure column 4, main condenser 5, first crude argon column 6 and the first crude argon overhead condenser 7 in addition.Main condenser is embodied as condenser-reboiler, is multilayer dipping bath formula evaporimeter (cascade evaporimeter) here especially.As substituting this, individual layer dipping bath formula evaporimeter or downward film evaporator can be adopted.Individual layer dipping bath formula evaporimeter (it also forms the condenser-reboiler with evaporation cavity and liquefaction chamber) uses in this as crude argon overhead condenser 7.
Secondly, main liquid state operation air stream 8 is at intermediate point supply high-pressure tower 3.At least part of liquid air is discharged again by pipeline 9, is crossing cooling in cool-heat-exchanger 10, and by pipeline 11 at intermediate point supply lower pressure column 4.
The sump liquid 12 of high-pressure tower is also crossing cooling in cool-heat-exchanger 10, and is supplied the evaporation cavity of the first crude argon overhead condenser by pipeline 13 and 14.Pipeline 14 is used as " cooling fluid being introduced the cooling line in the evaporation cavity of the first crude argon overhead condenser ".
Impure liquid nitrogen flows through pipeline 15 and discharges from the different intermediate points of high-pressure tower 3, is exported to the tower top of lower pressure column 4 by excessively cold (10) by pipeline 16.
The Part I 17 of the gaseous overhead nitrogen of high-pressure tower 3 is introduced into the liquefaction chamber of main condenser 5.The Part I 19 of the liquid nitrogen 18 produced in main condenser exports as the adverse current of high-pressure tower tower top.Part II 20 can be used as liquid form product by pipeline 21 and reclaims after crossing cold 10.The Part II 22 of the gaseous overhead nitrogen of high-pressure tower 3 can flow directly to main heat exchanger, and then reclaims as gaseous state pressurized product.
Liquid oxygen 23 is discharged from the storage tank of lower pressure column, and Part I 25 is transported in the evaporation cavity of main condenser 5 by pump 24.The gaseous oxygen 26 produced in main condenser returns the storage tank of lower pressure column in an identical manner as flushing liquid 27.Gaseous state not purity nitrogen 28 is discharged from the tower top of lower pressure column 4, heats, and flow to main heat exchanger by pipeline 29 in mistake cool-heat-exchanger.
The intermediate point of lower pressure column is communicated with the sump region of liquid back pipe road 31 with the first crude argon column 6 by supply air line 30.
The overhead gas 32 of the first crude argon column 6 is liquefied for the major part of the first crude argon overhead condenser.Liquid part flows back to the tower top of the first crude argon column 6 by pipeline 33 and is used as liquid adverse current here.Residual gas polymorphic segment 34 is discharged and in main heat exchanger in the first crude argon pipeline 34, is heated in any one at its passage or is heated together with not purity nitrogen 29.
The steam 34 produced in the evaporation cavity of the first crude argon overhead condenser and unevaporated liquid 35 are discharged from the evaporation cavity of the first crude argon overhead condenser, and are supplied to lower pressure column 4 at suitable intermediate point.
In this respect, the exemplary of ice chest 1 inside reclaims but the air-seperation system having argon to ooze out corresponding to traditional argon that do not have.
The preparation pipeline transforming argon reclaimer is provided in addition in framework of the present invention.Exemplary in Fig. 1 comprises following preparation pipeline (it illustrates in the drawings by a dotted line):
-for discharging the preparation pipeline 101 of the gaseous overhead product of the first crude argon column,
-for inserting the liquid into the second preparation pipeline 102 of the upper area of the first crude argon column,
-for discharging the 3rd preparation pipeline 103 of cooling fluid from distillation column system,
-for the cooling fluid of evaporation being introduced the 4th preparation pipeline 104 of the zone line of lower pressure column,
-for unevaporated cooling fluid being introduced the 5th preparation pipeline 105 of the zone line of lower pressure column, and selectively with
-for unevaporated cooling fluid being introduced the 6th preparation pipeline 106 of the zone line of lower pressure column.
Described preparation pipeline introduces the outer wall of the first ice chest 1, and comprises the flange being connected to pipeline pipeline in varied situations.The inoperation before transformation of preparation pipeline, but be blocked.
But if need argon to reclaim in the time after a while, then the modernization system comprising the second ice chest 40 of the second crude argon column 41 having suitable connecting line is added in the framework according to the inventive method for transformation.
In the exemplary of Fig. 1, modernization system comprises the second crude argon overhead condenser 42 in addition and has the pure argon column 43 of straight argon overhead condenser 44 and storage tank evaporimeter 46.Connecting line 201,202,203,204,205 is communicated with corresponding preparation pipeline 101 to 106 with 206 fluids.Pipeline 14 and 34 is blocked and is not operated.
Then, Overall Reconstruction system acts on as traditional air-seperation system with crude argon recovery in the Crude argon column system separated.Crude argon column is separately made up of " lower part " that formed by the first crude argon column 6 and " upper part " with the overhead condenser 42 formed by the second crude argon column 42.First crude argon overhead condenser no longer operates, but its evaporation cavity should be emptied completely or continuously be rinsed by little plume.
The overhead gas of the first crude argon column 6 is introduced into the sump region of the second crude argon column 41 by pipeline 101 and 201; The sump liquid of the second crude argon column 41 flows back to the tower top of the first crude argon column 6 in the opposite direction by storage tank 45 and pipeline 202 and 102.
The cold sump liquid 13 of mistake from high-pressure tower 4 no longer flow to the first crude argon overhead condenser 7 now, but flows into modernization system by pipeline 103 and 203.Once transmit sensible heat in the storage tank evaporimeter 46 of pure argon column, then excessively cold further stream is divided into two plumes 47 and 48, and this two plume is supplied to the evaporation cavity of two condenser-reboilers 42 and 44.From there, evaporation section 49/50 is supplied in lower pressure column 4 by pipeline 204 and 104, and the liquid of remainder passes through pipeline 205 and 105, or 206 and 106.The part 51 of the sump liquid of pure argon column 43 is discharged as liquid argon product.The residual gas 52 do not liquefied in overhead condenser 44 is output in air (ATM).
Fig. 2 illustrates the exemplary of the second distortion of the present invention.Difference with Fig. 1 is only described below.In addition, with the application similarly described in FIG.
The operation not having argon to reclaim the main system of (ice chest 1) in Fig. 2 does not have different from Fig. 1.But device comprises different preparation pipelines:
-the 7th preparation pipeline 301 for gas is discharged from the mid portion of lower pressure column,
-for inserting the liquid into the 8th preparation pipeline 302 of the mid portion of lower pressure column,
-for gas being introduced the 9th preparation pipeline 303 of the bottom section of the first crude argon column,
-the tenth preparation pipeline 304 for liquid is discharged from the bottom section of the first crude argon column,
-the 11 preparation pipeline 305 for the gaseous overhead product of the first crude argon column is discharged,
-the 12 preparation pipeline 306 for cooling fluid is discharged from distillation column system,
-for the cooling fluid of evaporation being introduced the 13 preparation pipeline 307 of the zone line of lower pressure column, and
-for unevaporated cooling fluid being introduced the 14 preparation pipeline 308 of the zone line of lower pressure column.
The difference of the modernization system in ice chest 40 is only the second crude argon overhead condenser lacking corresponding manner, other pump 60 and be different from those the circuit of connecting line 410 to 409 of Fig. 1.
After transformation process, the total system of Fig. 2 is used as conventional air piece-rate system in the crude argon column separated.Crude argon column is separately by " lower part " that formed by the second crude argon column 42 and form " upper part " with overhead condenser 7 by the first crude argon column 6 and form.
Claims (10)
1. the device for Cryogenic air separation, described device has distillation column system, described distillation column system comprises high-pressure tower (3), lower pressure column (4) and the first crude argon column (6), and be arranged at least one first ice chest (1), and described device has:
-for the supply air line (30) will introduce described first crude argon column (6) from the gas of the mid portion of described lower pressure column (4),
-for the liquid of described crude argon column (6) being introduced the liquid back pipe road (31) of the mid portion of described lower pressure column (4),
-for generation of the first crude argon overhead condenser (7) of the counter fluid for described first crude argon column (6), it is implemented as the condenser-reboiler with liquefaction chamber and evaporation cavity,
-for cooling fluid being introduced the cooling line (14) of the evaporation cavity of described first crude argon overhead condenser (7), and have
-for discharging the first crude argon pipeline (34) of the gaseous overhead product of described first crude argon column (6) from described distillation column system,
It is characterized in that
-for block described first crude argon pipeline equipment and
-for described first crude argon column (6) being connected to the preparation pipeline (101,102 of the second crude argon column; 301,302), wherein said preparation pipeline through described first ice chest (1) outer wall and make described first and second crude argon columns can be used as the distillation fraction be connected in series to be operated.
2. device as described in claim 1, is characterized in that
-for blocking the equipment of described cooling line (14) to described first crude argon overhead condenser (7),
-for discharging the first preparation pipeline (101) of the gaseous overhead product of described first crude argon column (6),
-for inserting the liquid into the second preparation pipeline (102) of the upper area of described first crude argon column (6), and
-for discharging the 3rd preparation pipeline (13) of the cooling fluid from described distillation column system.
3. device as described in claim 2, is characterized in that
-for the cooling fluid of evaporation being introduced the 4th preparation pipeline (104) of the zone line of described lower pressure column (4),
And especially,
-for unevaporated cooling fluid being introduced the 5th preparation pipeline (105) of the zone line of described lower pressure column (4), and/or optional existence
-the 6th preparation pipeline (106) of the zone line of described lower pressure column (4) is introduced for the unevaporated cooling fluid of the overhead condenser by pure argon column.
4. the device according to any one of Claims 1-4, is characterized in that
-for blocking the equipment of described supply air line (30) to described first crude argon column (6),
-for blocking the equipment from the liquid back pipe road (31) of described first crude argon column (6),
-for the 7th preparation pipeline (301) of the mid portion Exhaust Gas from described lower pressure column (4),
-for inserting the liquid into the 8th preparation pipeline (302) of the mid portion of described lower pressure column (4),
-for gas is introduced the bottom section of described first crude argon column (6) the 9th preparation pipeline (303) and
-for discharging the tenth preparation pipeline (304) from the liquid of the bottom section of described first crude argon column (6).
5. the device according to any one of Claims 1-4, is characterized in that
-for discharging the 11 preparation pipeline (305) of the gaseous overhead product of described first crude argon column (6),
-for discharging the 12 preparation pipeline (306) of the cooling fluid of described distillation column system,
-for the cooling fluid of evaporation being introduced the 13 preparation pipeline (307) of the zone line of described lower pressure column (6), and especially
-for the unevaporated cooling fluid of the overhead condenser from pure argon column being introduced the 14 preparation pipeline (308) of the zone line of described lower pressure column (4).
6. a modernization system for the device of transformation according to any one of Claims 1-4, is characterized in that
-the second crude argon column (41),
-be wherein provided with second ice chest (40) of described second crude argon column (41), and
-for described second crude argon column being connected to the connecting line (201-205) of the preparation pipeline (101-105) of described device, wherein said connecting line passes the outer wall of described second ice chest (2),
-wherein said connecting line (201-205) is implemented for being connected to preparation pipeline (101-105).
7., as described in claim 6 for transforming the modernization system of device as claimed in claim 2 or claim 3, it is characterized in that
-for the bottom section of described second crude argon column (41) being connected to one or two connecting lines (201,202) of described first and second connecting lines (101,102),
-for generation of the second crude argon overhead condenser (42) of the liquid counter-current for described second crude argon column (41), it is implemented as the condenser-reboiler with liquefaction chamber and evaporation cavity, and
-for the evaporation cavity of described second crude argon overhead condenser (42) is connected to described 3rd preparation pipeline (103) connecting line (203) and
-especially, for the cooling fluid evaporated of the evaporation cavity from described second crude argon overhead condenser (42) being introduced the connecting line (204) of the mid portion of described lower pressure column (4).
8., as described in claim 6 for transforming the modernization system of the device as described in claim 4 or 5, it is characterized in that
-for the bottom section of described second crude argon column (41) being connected to one or two connecting lines of the described 7th and the 8th preparation pipeline (301,302),
-for the bottom section of described second crude argon column (41) being connected to one or two connecting lines of the described 9th and the tenth preparation pipeline (303,304).
9. the modernization system for transforming device according to claim 4 according to any one of claim 6 to 8, is characterized in that the pure argon column (43) with pure argon column overhead condenser (44).
10., for transforming a method for the Cryognic air separation system not having argon to reclaim, the modernization system that it is characterized in that according to any one of claim 6 to 9 is close to the main system not having argon to reclaim and sets up, and described connecting line is connected to described main system.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP13002046 | 2013-04-18 | ||
| EP13002046.4 | 2013-04-18 | ||
| PCT/EP2014/000891 WO2014169989A1 (en) | 2013-04-18 | 2014-04-03 | Retrofittable device for low-temperature separation of air, retrofitting system, and method for retrofitting a low-temperature air separation system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105264317A true CN105264317A (en) | 2016-01-20 |
| CN105264317B CN105264317B (en) | 2019-02-12 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201480022093.6A Active CN105264317B (en) | 2013-04-18 | 2014-04-03 | Transformation device, modernization system and the method that Cryognic air separation system is transformed of Cryogenic air separation |
Country Status (4)
| Country | Link |
|---|---|
| EP (1) | EP2986924B1 (en) |
| CN (1) | CN105264317B (en) |
| PL (1) | PL2986924T3 (en) |
| WO (1) | WO2014169989A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111630335A (en) * | 2018-01-26 | 2020-09-04 | 乔治洛德方法研究和开发液化空气有限公司 | Air separation plant by cryogenic distillation |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3067650B1 (en) * | 2015-03-13 | 2018-04-25 | Linde Aktiengesellschaft | Installation and method for producing gaseous oxygen by cryogenic air decomposition |
| WO2023198307A1 (en) | 2022-04-14 | 2023-10-19 | Linde Gmbh | Process and apparatus for producing argon from crude argon |
| FR3135134B1 (en) * | 2022-04-27 | 2024-04-19 | Air Liquide | Method for increasing the capacity of an existing cryogenic distillation air separation apparatus and air separation apparatus |
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| CN1112999A (en) * | 1994-02-24 | 1995-12-06 | 林德股份公司 | Process and apparatus for the recovery of pure argon |
| CN1244651A (en) * | 1998-06-10 | 2000-02-16 | 气体产品与化学公司 | Method for producing argo from low temperature air by separation |
| EP1103772A1 (en) * | 1999-11-26 | 2001-05-30 | Linde Aktiengesellschaft | Device for producing argon |
| EP2026024A1 (en) * | 2007-07-30 | 2009-02-18 | Linde Aktiengesellschaft | Process and device for producing argon by cryogenic separation of air |
| CN103282733A (en) * | 2010-07-05 | 2013-09-04 | 乔治洛德方法研究和开发液化空气有限公司 | Apparatus and process for the separation of air by cryogenic distillation |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5235816A (en) * | 1991-10-10 | 1993-08-17 | Praxair Technology, Inc. | Cryogenic rectification system for producing high purity oxygen |
| EP1760415A1 (en) * | 2005-08-31 | 2007-03-07 | SIAD MACCHINE IMPIANTI S.p.a. | Process and device for the production of argon by cryogenic separation of air |
-
2014
- 2014-04-03 EP EP14715547.7A patent/EP2986924B1/en active Active
- 2014-04-03 WO PCT/EP2014/000891 patent/WO2014169989A1/en active Application Filing
- 2014-04-03 CN CN201480022093.6A patent/CN105264317B/en active Active
- 2014-04-03 PL PL14715547T patent/PL2986924T3/en unknown
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1112999A (en) * | 1994-02-24 | 1995-12-06 | 林德股份公司 | Process and apparatus for the recovery of pure argon |
| CN1244651A (en) * | 1998-06-10 | 2000-02-16 | 气体产品与化学公司 | Method for producing argo from low temperature air by separation |
| EP1103772A1 (en) * | 1999-11-26 | 2001-05-30 | Linde Aktiengesellschaft | Device for producing argon |
| EP2026024A1 (en) * | 2007-07-30 | 2009-02-18 | Linde Aktiengesellschaft | Process and device for producing argon by cryogenic separation of air |
| CN103282733A (en) * | 2010-07-05 | 2013-09-04 | 乔治洛德方法研究和开发液化空气有限公司 | Apparatus and process for the separation of air by cryogenic distillation |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111630335A (en) * | 2018-01-26 | 2020-09-04 | 乔治洛德方法研究和开发液化空气有限公司 | Air separation plant by cryogenic distillation |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105264317B (en) | 2019-02-12 |
| WO2014169989A1 (en) | 2014-10-23 |
| PL2986924T3 (en) | 2017-12-29 |
| EP2986924A1 (en) | 2016-02-24 |
| EP2986924B1 (en) | 2017-07-12 |
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