CN102692114A - Method and device for creating an oxygen product by cryogenic decomposition of air - Google Patents
Method and device for creating an oxygen product by cryogenic decomposition of air Download PDFInfo
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- CN102692114A CN102692114A CN201210120155XA CN201210120155A CN102692114A CN 102692114 A CN102692114 A CN 102692114A CN 201210120155X A CN201210120155X A CN 201210120155XA CN 201210120155 A CN201210120155 A CN 201210120155A CN 102692114 A CN102692114 A CN 102692114A
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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
- F25J3/04896—Details of columns, e.g. internals, inlet/outlet devices
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
- F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
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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
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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
- F25J3/04472—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 cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
- F25J3/04478—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 cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for controlling purposes, e.g. start-up or back-up procedures
- F25J3/0449—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 cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for controlling purposes, e.g. start-up or back-up procedures for rapid load change of the 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
- 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
- F25J3/04896—Details of columns, e.g. internals, inlet/outlet devices
- F25J3/04927—Liquid or gas distribution devices
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/10—Boiler-condenser with superposed stages
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The method involves cooling a feed air stream (3) in a main heat exchanger (2), where the cooling process is initiated in a high-pressure column (6). A liquid buffer (33) is arranged between the lower end of the lowermost mass transfer section of a low-pressure column (7) and a main condenser (8). The liquid buffer is designed for storage of liquid. The liquid is introduced into the liquid buffer from the bottom of the main condenser during load reduction. An independent claim is included for an apparatus for generating an oxygen product by low-temperature fractionation of air.
Description
Technical field
The present invention relates to produce the method and apparatus of oxygen product through low temperature air separating.
Background technology
For example the 2nd edition the 4th chapter of Hausen/Linde cryogenic technique 1985 (the 281st～337 page) just discloses the method and apparatus of low temperature air separating.
Can distillation column system of the present invention be designed to double tower system (for example traditional Linde double tower system), also can be designed to three towers or multitower system.System can also have and is used to obtain especially other devices of inert gas of high purity product and/or other composition of air except having nitrogen oxygen knockout tower, for example obtains argon gas and/or krypton-argon.
Lower pressure column has the operating pressure lower than high-pressure tower.In order to be created in the steam that rises in the mass exchange section; Lower pressure column has evaporimeter at the bottom of the tower; Be called main condenser; It is designed to the condenser-reboiler form, the mode of just carrying out heat exchange indirectly with liquid at the bottom of the tower of lower pressure column evaporation liquefy gaseous state heating fluid, for example the cat head nitrogen of high-pressure tower.Usually main condenser directly is arranged in (inboard main condenser) within the lower pressure column; Also can replace it is placed among the autonomous container outside the lower pressure column, and utilize pipeline its link to each other with lower pressure column (outside main condenser).
Each " condenser-reboiler " includes liquefied room and the vaporization chamber that is made up of liquefier channel and evaporation channel, condensation first fluid stream in liquefied room, and evaporation second fluid stream in vaporization chamber, this two fluid streams stream carries out heat exchange indirectly.Passage through there being heat exchange relationship each other constitutes vaporization chamber and liquefied room.
Can main condenser be designed to falling film evaporator or flooded evaporator (Badverdampfer).The present invention relates to main condenser is designed to the air separating method of flooded evaporator; Heat exchanger module in the said flooded evaporator (being also referred to as circulating evaporator or thermal siphon evaporimeter sometimes) is among the bath of liquid groove of fluid to be evaporated; Utilize thermosyphon effect to make fluid to be evaporated flow through evaporation channel from bottom to top, flow out again as two-phase mixture up then.Remaining liquid is flowing back into outside the heat exchanger module among the bath of liquid groove.(vaporization chamber of said flooded evaporator not only comprises evaporation channel, and comprises the peripheral space around the heat exchanger module).Falling film evaporator is then opposite, need take addition thereto to make the liquid of process evaporation channel overturn.
Also can use these two or more flooded evaporators that are arranged in juxtaposition as main evaporator, then with its evaporation side and the parallel connection of liquefaction side.Can the unique flooded evaporator that in these flooded evaporators each perhaps constitutes main evaporator be designed to the single or multiple lift pattern." multilayer flooded evaporator " has this two or more stacked layers up and down, realizes these layers through heat exchanging segment respectively.Can pass through independently each layer of heat exchanger module realization, perhaps the segmentation through same heat exchanger module constitutes at least two layers or all layers.Not only can evaporation side and also can liquefaction side with these layers serial or parallel connection.
A kind of particular embodiment of multilayer flooded evaporator is " a tandem type evaporimeter ", is in evaporation side layer to be connected here, and just unevaporated liquid flows to one deck down from last layer.Equally preferably in the liquefaction side with the tandem type evaporator series, for example through passing through the liquefier channel of all layers in the same heat exchanger module.Also can the layer of tandem type evaporimeter is parallelly connected in the liquefaction side.
" main heat exchanger " can be made up of the heat exchanging segment of one or more parallel connections and/or series connection, for example can be made up of one or more plate heat exchanger modules.
The said monograph of Hausen/Linde discloses the technical process that adopts the individual layer flooded evaporator.DE 1152432, DE 1949609A, WO 01/92798 A2, EP 1287302B1 and DE 102,007 003 437 A1 all disclose these class methods that adopt the multilayer flooded evaporator.
Summary of the invention
The object of the present invention is to provide a kind of method and corresponding apparatus that especially can when load changes fast, allow system stable operation.
Load variations is a kind of ruuning situation, and at this moment equipment be in the unstable transition stage from first change of production of oxygen product to second output.When " load improve ", second output is higher than first output; When " load reduces ", second output is lower than first output.
This purpose is to be used for distillation column system that separating nitrogen oxygen separates through utilization to realize through the variable method of producing living oxygen product with variable mode of low temperature air separating; Said distillation column system has high-pressure tower (6) and the lower pressure column (7) that all comprises the mass exchange section, wherein
-feed air stream (1,3,5) is cooled down in main heat exchanger (2), and import in the high-pressure tower (6),
-the product stream (28) of oxygen coalescence is discharged from the bottom of lower pressure column (7), at main heat exchanger
(2) heating in, and as oxygen product (29) acquisition,
-will import from the liquid that the nethermost mass exchange section (32) of lower pressure column (7) flows out the main condenser (8) of making flooded evaporator and condenser-reboiler structure, and in the main condenser vaporized in part, reach
-with unevaporated liquid from (35) at the bottom of main condenser (8) imports tower, the method is characterized in that,
-between the lower end of the nethermost mass exchange section (32) of lower pressure column (7) and main condenser (8), be provided with the liquid buffer (33) that is used for storaging liquid,
-during load reduces, liquid (32) at the bottom of the tower of main condenser is imported liquid buffer
(33) in and in this storage, increased the stored contents thing of liquid buffer (33) in the case, and
-the liquid that during load improves, at least a portion is stored in the liquid buffer (33) imports in (34) main condenser (8), has reduced the stored contents thing of liquid buffer (33) in the case.
According to another aspect of the present invention, it also provides the equipment of producing oxygen product through low temperature air separating, its
-having the distillation column system that is used for the separation of nitrogen oxygen, said distillation column system has high-pressure tower (6) and the lower pressure column (7) that all comprises the mass exchange section,
-have a main heat exchanger (2) that is used to cool off feed air stream (1,3,5),
-have a device that is used for the feed air stream through cooling is imported high-pressure tower (6),
-have and be used for discharging the product stream (28) of oxygen coalescence and it is imported the device of main heat exchanger (2) from the bottom of lower pressure column (7),
-have an oxygen product pipeline that is used for obtaining as oxygen product (29) through the product stream of heating,
-have a main condenser (8) as flooded evaporator and condenser-reboiler structure,
-have the device that is used for the liquid that the nethermost mass exchange section (32) from lower pressure column (7) flows out is imported main condenser (8), reach
-having and be used to collect at the bottom of the tower of the unevaporated liquid of main condenser (8) (35), this equipment is characterised in that
-be arranged on lower end and the liquid buffer (33) between the main condenser (8) of the nethermost mass exchange section (32) of lower pressure column (7),
-be used for liquid is imported the device of liquid buffer (33),
-the liquid that is used at least a portion is stored in liquid buffer (33) imports the device in (34) main condenser (8), and
-adjusting device; It is designed to during load reduces liquid (32) at the bottom of the tower of main condenser is imported the liquid buffers (33) and in this storage; Increased the stored contents thing of liquid buffering apparatus (33) in the case; And the liquid that during load improves, at least a portion is stored in the liquid buffer (33) imports in (34) main condenser (8), has reduced the stored contents thing of liquid buffer (33) in the case.
According to according to the invention, a liquid buffer is arranged in main condenser top, this can inject suitable liquid in the steady state operation of this method, a part of withdrawing fluid that for example flows out the mass exchange section below from lower pressure column.For example can in steady state operation, slowly inject liquid buffer, thereby under the unstable state ruuning situation that load improves, have the liquid of buffering available.According to according to the invention; Especially can be during load reduces liquid be sent at the bottom of the tower of main condenser among the liquid buffer; And improve the stored contents thing of liquid buffer, just send into liquid among the liquid buffer more than the liquid of therefrom discharging.
Among during load improves, then liquid being sent to main condenser from liquid buffer, and reduce the stored contents thing of liquid buffer, the liquid of just from liquid buffer, discharging is more than the liquid of sending into wherein.
Compare with falling film evaporator, the major advantage of flooded evaporator is not need the outside liquid circulation.As if this type of how unreasonable at a glance from the artificial eye-liquid endless form to buffer unit at the bottom of the tower, but the present invention finds that but this type of technological benefit is quite big, is worthy of the extra charge that is increased.
System of the present invention in addition reduces in the process also beneficial at load; Many low-purity liquid that can under this type of situation, will from the top mass exchange section of lower pressure column, flow out part at least is trapped among the buffer unit, thereby prevents or reduce the contaminating impurity of liquid at the bottom of the tower.
Under the unstable state service condition; For example when load variations, the heat exchanger effectiveness on the main condenser can reduce usually, and the present invention finds that reason is that evaporation side lacks liquid; Can utilize method of the present invention to replenish the liquid that lacks from buffer unit now; Therefore even under extreme service condition, for example when the per minute rate of load change occurring and change greater than centesimal quick load, equipment also can especially stably move and not have fault.
Liquid buffer suitably is arranged in the nethermost mass exchange section of lower pressure column below and main condenser top, makes that liquid can be at the vaporization chamber that flow into main condenser under the natural gravity effect from buffer unit perhaps among its last layer.For example can perhaps constitute liquid buffer through being arranged in one or more tower tray (for example annular tower tray) on the tower wall through one or more riser tower trays.
Usually constitute " at the bottom of the tower " of individual layer flooded evaporator through the bath of liquid groove.If the multilayer flooded evaporator, use nethermost bath of liquid groove as tower usually at the bottom of.Also can replace at the bottom of the separate space formation tower through the main condenser below.
Also can under the steady-state operation situation, adopt from the bottom of the tower to the liquid endless form of liquid buffer, at this moment need not to increase the stored contents thing; Under this type of situation, in the flooded evaporator and uncommon this type of circulation be used in the purity difference in the evaporimeter altitude range inner equilibrium evaporating liquid.Especially can in the multilayer flooded evaporator, realize stable especially operation.
According to the another kind of embodiment of the method for the invention, utilize the liquid pump that liquid is sent at the bottom of the tower of main condenser among the liquid buffer.
Because liquid buffer is above main condenser, but at the bottom of the tower but thereunder or in the lower end, therefore must the rising tower at the bottom of liquid could arrive liquid buffer.The method of any liquid that is used to raise can be used in principle, especially the liquid pump can be used.
The present invention is suitable for the multilayer flooded evaporator especially, and is if main condenser is designed to the tandem type evaporimeter, then useful.Employing not only can prevent to lack liquid from the liquid endless form to buffer unit at the bottom of the tower, but but also the concentration difference on the evaporation side of balance different layers (evaporation stage).Each evaporation stage of tandem type evaporimeter all can play the part evaporation, that is to say, oxygen concentration and evaporating temperature increase from top to bottom gradually.But flowing at the liquefaction side in fact constant nitrogen of condensing temperature that grows on trees, so the top evaporation stage of tandem type evaporimeter is basically with the temperature difference work bigger than below evaporation stage.When load variations, above will making, this lacks liquid more in evaporation stage, because the heat that these evaporation stages transform is more than the below evaporation stage.This embodiment according to the present invention is said; Now will be among the liquid juice at the bottom of the below evaporation stage flows out to tower be upwards sent into buffer unit again; Then from being sent to the evaporation stage of the top here; This evaporation stage is the lower purity of equilibrium ratio here; Generally can be in the altitude range of tandem type evaporimeter produce milder CONCENTRATION DISTRIBUTION, can offset two kinds of negative effects in the tandem type evaporimeter running simultaneously, promptly lack in liquid and the main condenser altitude range and undesired concentration difference during load variations in evaporation side.
If the product of oxygen coalescence stream has below 98% for example 90 to 95% oxygen concentration, then suitablely especially use method of the present invention.(if do not have other explanations, then be mole with all percentage values of the following stated here).
Especially can utilize two kinds of operational modes to carry out this method; Under first kind of operational mode, send into liquid in the liquid buffer more than the liquid of therefrom discharging, the liquid of under second kind of operational mode, from liquid buffer, discharging is more than the liquid of sending into wherein.For example first kind of operational mode is equivalent to the constant steady-state operation of loading; Second kind of operational mode is equivalent to the load variations situation, for example becomes the transition period raising load of second steady state operating condition with higher second output from first steady state operating condition with first output.
Description of drawings
Shown in Figure 1 is sketch map according to air separation equipment of the present invention.
The specific embodiment
Below will carry out illustrated in detail to the present invention and other details of the present invention according to the embodiment shown in the sketch map.
Feeding air 1 through overcompression and purification is gone into the hot junction of main heat exchanger 2 with the pressure current of about 5.5 crust, and is divided into 3 and second strands of air streams 4 of first strand of air stream.Can tell a part of dry air 1 through pipeline 5 and perhaps be supplied to other pneumatic plants as instrument air.
In main heat exchanger 2, first strand of air stream 3 roughly is cooled to dew point; Send among the high-pressure tower 6 through pipeline 5 then; High-pressure tower is a part that is used for the distillation column system of separating nitrogen oxygen, and this system comprises a lower pressure column 7 and a main condenser 8 that is designed to the tandem type evaporimeter.Operating pressure in these towers (respectively on cat head): be about 5.2 crust in the high-pressure tower 6, be about 1.3 crust in the lower pressure column 7.
In main heat exchanger 2, second strand of air stream 4 only is cooled to medium temperature; And under medium temperature, send into and utilize generator 10 its eddy expansion machine of braking 9; Make its acting roughly pressure of lower pressure column that reduces pressure here; Again send back to main heat exchanger 2 through pipeline 11, finally send into lower pressure column 7 through pipeline 12 in a certain middle part.
The cat head nitrogen of high-pressure tower 6 13 parts 14 are sent into the liquefied room of main condenser 8, in main heat exchanger 2, remainder 15 roughly is heated to environment temperature, finally discharge as gaseous nitrogen compressed product (PGAN) through pipeline 16.
The first 18 of the liquid nitrogen 17 that produces in the main condenser 8 is sent into the cat head of high-pressure tower 6 as backflow, second portion 19 is cooled down in reverse-flow subcooler 23, send into the cat head of lower pressure column 7 then through pipeline 20 as backflow.Can third part 21 be discharged as liquid nitrogen product (LIN) in case of necessity.
With the cooling in reverse-flow subcooler 23 equally of liquid 24 at the bottom of the tower of the oxygen coalescence of high-pressure tower 6, then a certain middle part is sent to lower pressure column 7 through pipeline 25 among.
Discharge gaseous nitrogen 26 from the cat head of lower pressure column 7, in reverse-flow subcooler 23 and main heat exchanger 2, be heated, discharge through pipeline 27 then, in the air cleaning unit of for example not drawing in the drawings it is used as regeneration gas.
Discharge the product stream 28 of oxygen coalescence from the bottom (here directly above main condenser 8) of lower pressure column 7, in main heat exchanger 2, it roughly is heated to environment temperature, obtain oxygen product (GOX) through pipeline 29 then.Can 35 obtain a part of liquid at the bottom of the tower of main condenser 8 through pipeline 30,31,33 and pump 32, for example be used for filling the usefulness of wet tank in order to emergent supply as product liquid (LOX).
As substituting or additional project, except taking out gaseous products, also can obtain the pressure oxygen product through the internal compression mode, method is that a part of liquid oxygen 31 is exerted pressure, and in main heat exchanger 2, makes its evaporation or false evaporation then.
According to according to the invention, there is the liquid buffer 33 of an annular column disk-form to be located immediately at lower pressure column 7 nethermost mass exchange sections 32 belows.In the equipment steady state operation, can a part of liquid from nethermost mass exchange section 32 outflows be charged among this liquid buffer.Among through pipeline 34 liquid being sent into main condenser 8 from buffer unit 33 orientations under the situation that load improves, and be to send among the bath of liquid groove of its superiors.
In any case all can be when load reduces liquid 36 be sent among the liquid buffer 33 at the bottom of the tower through liquid pump 36 and pipeline 37.
Claims (7)
1. be used for the method that distillation column system that nitrogen oxygen separates is produced oxygen product through low temperature air separating with variable mode, said distillation column system has high-pressure tower (6) and the lower pressure column (7) that all comprises the mass exchange section, wherein
-feed air stream (1,3,5) is cooled off in main heat exchanger (2), and import in the high-pressure tower (6),
-the product stream (28) of oxygen coalescence is discharged from the bottom of lower pressure column (7), heating in main heat exchanger (2), and as oxygen product (29) acquisition,
-will import from the liquid that the nethermost mass exchange section (32) of lower pressure column (7) flows out the main condenser (8) as flooded evaporator and condenser-reboiler structure, and in the main condenser vaporized in part, reach
-with unevaporated liquid from (35) at the bottom of main condenser (8) imports tower, the method is characterized in that,
-between the lower end of the nethermost mass exchange section (32) of lower pressure column (7) and main condenser (8), be provided with the liquid buffer (33) that is used for storaging liquid,
-during load reduces, liquid (32) at the bottom of the tower of main condenser is imported the liquid buffers (33) and in this storage, increased the stored contents thing of liquid buffer (33) in the case, and
-the liquid that during load improves, at least a portion is stored in the liquid buffer (33) imports in (34) main condenser (8), has reduced the stored contents thing of liquid buffer (33) in the case.
2. according to the method for claim 1, it is characterized in that, utilize liquid pump (36) that liquid (35) at the bottom of the tower of main condenser is imported the liquid buffers (33).
3. according to the method for claim 2, it is characterized in that main condenser (8) is especially constructed as the tandem type evaporimeter as the multilayer flooded evaporator.
4. according to the method for claim 3, it is characterized in that the oxygen concentration of the product stream (28) of oxygen coalescence is less than 98%.
5. produce the equipment of oxygen product through low temperature air separating, its
-having the distillation column system that is used for the separation of nitrogen oxygen, said distillation column system has high-pressure tower (6) and the lower pressure column (7) that all comprises the mass exchange section,
-have a main heat exchanger (2) that is used to cool off feed air stream (1,3,5),
-have a device that is used for the feed air stream through cooling is imported high-pressure tower (6),
-have and be used for discharging the product stream (28) of oxygen coalescence and it is imported the device of main heat exchanger (2) from the bottom of lower pressure column (7),
-have an oxygen product pipeline that is used for obtaining as oxygen product (29) through the product stream of heating,
-have a main condenser (8) as flooded evaporator and condenser-reboiler structure,
-have the device that is used for the liquid that the nethermost mass exchange section (32) from lower pressure column (7) flows out is imported main condenser (8), reach
-having and be used to collect at the bottom of the tower of the unevaporated liquid of main condenser (8) (35), this equipment is characterised in that
-be arranged on lower end and the liquid buffer (33) between the main condenser (8) of the nethermost mass exchange section (32) of lower pressure column (7),
-be used for liquid is imported the device of liquid buffer (33),
-the liquid that is used at least a portion is stored in liquid buffer (33) imports the device in (34) main condenser (8), and
-adjusting device; It is designed to during load reduces liquid (32) at the bottom of the tower of main condenser is imported the liquid buffers (33) and in this storage; Increased the stored contents thing of liquid buffer (33) in the case; And the liquid that during load improves, at least a portion is stored in the liquid buffer (33) imports in (34) main condenser (8), has reduced the stored contents thing of liquid buffer (33) in the case.
6. according to the equipment of claim 5, it has the liquid pump (36) that is used for liquid (35) at the bottom of the tower of main condenser is transported to liquid buffer (33).
7. according to the equipment of claim 6, it is characterized in that main condenser (8) is especially constructed as the tandem type evaporimeter as the multilayer flooded evaporator.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP11002364.5 | 2011-03-22 | ||
| EP11002364 | 2011-03-22 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102692114A true CN102692114A (en) | 2012-09-26 |
Family
ID=44583651
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210120155XA Pending CN102692114A (en) | 2011-03-22 | 2012-03-21 | Method and device for creating an oxygen product by cryogenic decomposition of air |
Country Status (3)
| Country | Link |
|---|---|
| US (1) | US20120240620A1 (en) |
| EP (1) | EP2503270A1 (en) |
| CN (1) | CN102692114A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2022258222A1 (en) * | 2021-06-07 | 2022-12-15 | Linde Gmbh | Air separation plant and air separation method |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1152432B (en) | 1962-04-21 | 1963-08-08 | Linde Eismasch Ag | Plate condenser evaporator, especially for gas and air separators |
| DE1949609C3 (en) | 1969-10-01 | 1978-05-11 | Linde Ag, 6200 Wiesbaden | Condenser evaporator for a double column rectifier |
| WO1990000243A1 (en) * | 1988-07-04 | 1990-01-11 | Japan Oxygen Co., Ltd. | Condenser/evaporator |
| DE4415747C2 (en) * | 1994-05-04 | 1996-04-25 | Linde Ag | Method and device for the low-temperature separation of air |
| JPH1054656A (en) * | 1996-08-12 | 1998-02-24 | Nippon Sanso Kk | Air liquefying and separating device and method thereof |
| DE10027139A1 (en) | 2000-05-31 | 2001-12-06 | Linde Ag | Multi-storey bathroom condenser |
| DE10027140A1 (en) | 2000-05-31 | 2001-12-06 | Linde Ag | Multi-storey bathroom condenser |
| DE102005028012A1 (en) * | 2005-06-16 | 2006-09-14 | Linde Ag | Separation of air into nitrogen and oxygen at low temperatures, with a distillation column system, uses liquefied natural gas |
| DE102007003437A1 (en) | 2007-01-23 | 2007-09-20 | Linde Ag | Condenser bath used as the primary condenser in cryogenic fractionation plant, comprises quadrangular condenser blocks having evaporation passages for liquid and liquefaction passages for heating medium, and liquid supply container |
-
2012
- 2012-03-01 EP EP12001386A patent/EP2503270A1/en not_active Withdrawn
- 2012-03-21 CN CN201210120155XA patent/CN102692114A/en active Pending
- 2012-03-21 US US13/425,569 patent/US20120240620A1/en not_active Abandoned
Also Published As
| Publication number | Publication date |
|---|---|
| EP2503270A1 (en) | 2012-09-26 |
| US20120240620A1 (en) | 2012-09-27 |
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Application publication date: 20120926 |