CN105910388A - Air separation device and air separation method - Google Patents
Air separation device and air separation method Download PDFInfo
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- CN105910388A CN105910388A CN201610392029.8A CN201610392029A CN105910388A CN 105910388 A CN105910388 A CN 105910388A CN 201610392029 A CN201610392029 A CN 201610392029A CN 105910388 A CN105910388 A CN 105910388A
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- air
- rectifying column
- oxygen
- separation equipment
- enriched liquid
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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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
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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
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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
- F25J3/04418—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 with thermally overlapping high and low pressure columns
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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
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/34—Processes or apparatus using separation by rectification using a side column fed by a stream from the 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
- F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
Abstract
The invention provides an air separation device and an air separation method. The air separation device comprises a compressor and a double-level rectifying tower. The double-level rectifying tower comprises an upper rectifying tower body, a lower rectifying tower body and a condensation evaporator arranged between the upper rectifying tower body and the lower rectifying tower body. An oxygen-enriched liquid air inlet is formed in the middle portion of the upper rectifying tower body. The compressor is connected with the middle portion of the upper rectifying tower body through a first air conveying pipeline, and a connector of the compressor is located below the oxygen-enriched liquid air inlet. The top of the lower rectifying tower body is connected with the condensation evaporator through a nitrogen conveying pipeline. The air separation device further comprises a third rectifying tower body, and the third rectifying tower body is connected with the bottom of the upper rectifying tower body through a second oxygen-enriched liquid air conveying pipeline to convey second oxygen-enriched liquid air generated by the upper rectifying tower body to the third rectifying tower body for rectification. An evaporator is arranged at the bottom of the third rectifying tower body and provided with an air inlet and an air outlet. The air inlet is connected with the compressor through a second air conveying pipeline, and the air outlet is connected with the lower rectifying tower body. The exhaust pressure of the compressor is reduced, and energy saving is achieved.
Description
Technical field
The present invention relates to technical field of air separation, in particular to a kind of air separation equipment and air separating method.
Background technology
It is oxidant source that combustion process traditionally is all based on greatly air, and the oxygen of i.e. 21% participates in combustion process, and in air
Nitrogen adsorption amount of heat, after discharge as flue gas, cause waste of fuel.Along with the development of combustion technology, oxygen-enriched sky
Gas is as the more energy efficient environmental protection of combustion process of oxidant；Under oxygen enriched environment, fuel combustion is thorough, and heat is fully discharged,
Reduce the heat loss of fuel, and oxygen-enriched energy consumption is less than pure oxygen.In recent years, using the oxygen-enriched type of furnace proportion as oxidant
It is stepped up.
The primarily discrete air of preparation method of industry oxygen-enriched air at present, most widely used is cryogenic rectification method.Traditional method
Having two kinds, one is to produce pure oxygen, is blended into air, blendes together required oxygen-rich concentration, this first separates the side mixed afterwards
Formula is undoubtedly the waste of a kind of energy；The second is low as disclosed in the application for a patent for invention of Application No. 201110096197.X
Pressure oxygen-enriched air separating technology, its flow process is that double tower positive flowrate expansion produces oxygen enriching process, specifically includes below scheme:
(1) air is filtered remove impurity, enters air compressor machine and is compressed to 0.38-0.44MPa, is subsequently cooled to 5-10 DEG C, continues
Continuous molecular sieve adsorber of sending into purifies；(2) air after purifying divides two-way, and a road enters space division fractional distillation as expanded air
The expansion gas passage of tower main heat exchanger, then by extracting entrance expander in the middle part of main heat exchanger out, another road air is directly through master
Heat exchanger is cooled to dew point temperature, enters back into tower rectification under space division fractionating column, under space division fractionating column at the bottom of tower after continuing on through oxygen evaporator
Portion obtains oxygen-enriched liquid air, and under space division fractionating column, top of tower obtains nitrogen；(3) oxygen-enriched liquid air of tower bottom and top under space division fractionating column
Portion nitrogen condensation liquid nitrogen after cooler is supercool with expander after air respectively enter tower rectification, space division on space division fractionating column
On fractionating column, top of tower obtains nitrogen；(4) liquid oxygen that on space division fractionating column, tower bottom obtains enters oxygen evaporator by from main heat exchange
The air of device heats and vaporizes, and oxygen pressure improves to 65-80KPa, obtains oxygen product after main heat exchanger re-heat.
In actual applications, although its more general space division of air compressor machine row pressure relatively low (about 0.38MPa), but due to by main cold temperature
The restriction of difference, it is impossible to reduce further, the most energy-conservation to realize.
Summary of the invention
Present invention is primarily targeted at a kind of air separation equipment of offer and air separating method, to solve prior art hollow
The problem of edema caused by disorder of QI separating process energy-saving effect difference.
To achieve these goals, according to an aspect of the invention, it is provided a kind of air separation equipment, including: compressor；
Double rectification column, double rectification column includes rectifying column, lower rectifying column and the condensation being arranged between rectifying column and lower rectifying column
Vaporizer, the middle part of upper rectifying column has oxygen-enriched liquid air import, and compressor passes through the first air delivery pipe with the middle part of upper rectifying column
Road is connected and interface is positioned at below oxygen-enriched liquid air import, and the top of lower rectifying column is connected by nitrogen transfer pipeline with condenser/evaporator
So that nitrogen enters the condensation side of condenser/evaporator and heats second oxygen-enriched liquid air of evaporation side of condenser/evaporator, the second oxygen-rich liquid
Empty from upper rectifying column, nitrogen also includes from lower rectifying column, air separation equipment: the 3rd rectifying column, with the end of upper rectifying column
Portion is delivered to the 3rd rectifying column by connected the second oxygen-enriched liquid air produced by upper rectifying column of the second oxygen-enriched liquid air transfer pipeline and carries out essence
Evaporating, the bottom of the 3rd rectifying column is provided with vaporizer, and vaporizer has air intake and air outlet slit, air intake and compressor
Being connected by the second air delivery pipe, air outlet slit is connected with lower rectifying column.
Further, the above-mentioned top of the 3rd rectifying column is connected and interface by top gas transfer pipeline with the middle part of upper rectifying column
It is positioned at below oxygen-enriched liquid air import.
Further, the bottom of above-mentioned lower rectifying column and the oxygen-enriched liquid air import of upper rectifying column are by the first oxygen enriched liquid transfer pipeline
It is connected.
Further, above-mentioned air separation equipment also includes: subcooler, is arranged on the first oxygen enriched liquid transfer pipeline.
Further, above-mentioned condenser/evaporator condensation side is connected by liquid nitrogen transfer pipeline with the top of upper rectifying column, and liquid nitrogen is defeated
Send pipeline to pass subcooler to arrange.
Further, above-mentioned air separation equipment also includes: main heat exchanger, is arranged on the second air delivery pipe.
Further, above-mentioned upper rectifying column top connects has product nitrogen gas output pipe, product nitrogen gas output pipe to sequentially pass through
Cooler and main heat exchanger are arranged.
Further, above-mentioned 3rd rectifier bottoms connects oxygen rich gas product transfer pipeline, oxygen rich gas product transfer pipeline
Arrange through main heat exchanger.
Further, above-mentioned air separation equipment also includes: pre-cooling purification unit, and the first air delivery pipe is sequentially connected with compression
Machine, pre-cooling purification unit, the middle part of upper rectifying column, the second air delivery pipe be sequentially connected with compressor, pre-cooling purification unit and
Air intake, the first air delivery pipe and the second air delivery pipe merge between the outlet and compressor of pre-cooling purification unit
Arrange.
Further, above-mentioned air separation equipment also includes: booster expansion machine, has pressurized end and an expanding end, pressurized end and swollen
Swollen end is successively set on the first air delivery pipe according to air flow, and is arranged on main heat exchanger according to air flow expanding end
Downstream；Cooler, is arranged on the first air delivery pipe and between pressurized end and main heat exchanger.
According to a further aspect in the invention, it is provided that a kind of air separating method, above-mentioned air separation equipment is used to carry out air
Separate, wherein, utilize the double rectification column of air separation equipment upper rectifying column obtain oxygen content be 70～82% second rich
Oxygen liquid air；Second oxygen-enriched liquid air obtains gas products and the oxygen content of oxygen content more than 90% through the rectification of the 3rd rectifying column
The fluid product of more than 95%.
Application technical scheme, the road air from compressor enters upper rectifying column 83 through the first air delivery pipe,
And in upper rectifying column, obtain the second oxygen-enriched liquid air and top nitrogen, when upper rectifying column rectification, control its rectification condition and make second
The oxygen content of oxygen-enriched liquid air, less than the oxygen content of prior art, is such as 70～82%, and the second oxygen-enriched liquid air enters condenser/evaporator
Evaporation side and the nitrogen being positioned at condensation side carry out heat exchange；Another road air enters the 3rd rectifying column through the second air delivery pipe
Vaporizer, in order to provide the upflowing vapor needed for the 3rd rectifying column rectification, and self is entered by the lower rectifying column of entrance after partial liquefaction
Row rectification；In lower rectifying column, the air of partial liquefaction obtains the first oxygen-enriched liquid air and top nitrogen after being distillated；Top nitrogen is led to
Cross nitrogen transfer pipeline and be conveyed into the condensation side of condenser/evaporator, and heat the second oxygen-enriched liquid air of the evaporation side of this condenser/evaporator,
And the rear section backflow as lower rectifying column that self is condensed, part is as upper rectifier column reflux liquid.Steam owing to being positioned at this condensation
The oxygen content of the second oxygen-enriched liquid air sending out device is low so that the evaporating temperature at condenser/evaporator reduces, so that condenser/evaporator
Condensation temperature reduce, and then cause lower Rectification column pressure to reduce, further such that the row pressure reduction of compressor, and compressor
Row pressure reduces the most energy-conservation for realization.On the basis of achieving above-mentioned energy-saving effect, utilize the second oxygen-enriched liquid air conveying pipe
Relatively low the second oxygen-enriched liquid air being unsatisfactory for product demand of oxygen content that upper rectifying column is produced by road is conveyed into the 3rd rectifying column and carries out essence
Evaporate, and then be met the oxygen enriched product of product demand.Simultaneously because, air is higher than nitrogen condensation temperature at the same pressure,
Air goes out the state of vaporizer gas-liquid two-phase simultaneously, and under this state, the bubble point temperature of temperature condensation more complete than air is high, thus reaches
While Compressor Discharge Pressure reduces, it is ensured that the heat transfer temperature difference of vaporizer, meet the 3rd rectifying column at rectification the second oxygen-enriched liquid air
Upflowing vapor required for during.As can be seen here, the application is by controlling its rectification condition during rectifying column in application, it is achieved
Reduce the row pressure of compressor, and then achieve energy-conservation purpose；Meanwhile, the oxygen that upper rectifying column is produced by the 3rd rectifying column is utilized
Relatively low the second oxygen-enriched liquid air of content carries out further rectification, has obtained the oxygen enriched product that oxygen content is higher.The application is obtaining richness
While oxygen product, it is possible to produce nitrogen and partially liq product, product category is enriched, and improves production capacity benefit further.
Accompanying drawing explanation
The Figure of description of the part constituting the application is used for providing a further understanding of the present invention, and the present invention's is schematic real
Execute example and illustrate for explaining the present invention, being not intended that inappropriate limitation of the present invention.In the accompanying drawings:
Fig. 1 shows the schematic diagram of the air separation equipment structure of the offer according to the present invention.
Wherein, above-mentioned accompanying drawing includes the following drawings labelling:
10, air filter；20, compressor；30, pre-cooling purification unit；31, pre-cooler；32, purification devices；40、
Booster expansion machine；41, pressurized end；42, expanding end；50, cooler；60, main heat exchanger；70, subcooler；81, under
Rectifying column；82, condenser/evaporator；83, upper rectifying column；90, the 3rd rectifying column；91, vaporizer；101, the first air is defeated
Send pipeline；102, nitrogen transfer pipeline；103, the second oxygen-enriched liquid air transfer pipeline；104, the second air delivery pipe；105、
Top gas transfer pipeline；106, the first oxygen enriched liquid transfer pipeline；107, liquid nitrogen transfer pipeline；108, product nitrogen gas output
Pipeline；109, oxygen rich gas product transfer pipeline；110, dirty nitrogen transfer pipeline.
Detailed description of the invention
It should be noted that in the case of not conflicting, the embodiment in the application and the feature in embodiment can be mutually combined.
Describe the present invention below with reference to the accompanying drawings and in conjunction with the embodiments in detail.
As described in background technology, due to the restriction of air separation equipment in prior art, its air that can implement is caused to divide
The energy-saving effect of separating process is poor.In order to solve this problem, in a kind of typical embodiment of the application, it is provided that Yi Zhongkong
Gas separation equipment, this air separation equipment includes compressor 20 and double rectification column, double rectification column include rectifying column 83, under
Rectifying column 81 and the condenser/evaporator 82 being arranged between rectifying column 83 and lower rectifying column 81, the middle part tool of upper rectifying column 83
Oxygen-enriched liquid air import, compressor 20 is had to be connected and interface position by the first air delivery pipe 101 with the middle part of upper rectifying column 83
Below oxygen-enriched liquid air import, the top of lower rectifying column 81 and condenser/evaporator 82 be connected by nitrogen transfer pipeline 102 so that
Nitrogen enters the condensation side of condenser/evaporator 82 and heats second oxygen-enriched liquid air of evaporation side of condenser/evaporator 82, and second is oxygen-enriched
Liquid air is from upper rectifying column 83, and nitrogen is from lower rectifying column 81, and this air separation equipment also includes the 3rd rectifying column 90, the 3rd essence
Evaporate tower 90 and the bottom of upper rectifying column 83 to be connected second produced by upper rectifying column 83 by the second oxygen-enriched liquid air transfer pipeline 103
Oxygen-enriched liquid air is delivered to the 3rd rectifying column 90 and carries out rectification, and the bottom of the 3rd rectifying column 90 is provided with vaporizer 91, vaporizer 91
Having air intake and air outlet slit, air intake is connected by the second air delivery pipe 104 with compressor 20, air outlet slit
It is connected with lower rectifying column 81.
A road air from compressor enters upper rectifying column 83 through the first air delivery pipe 101, and in upper rectifying column 83
Obtain the second oxygen-enriched liquid air and top nitrogen, when upper rectifying column 83 rectification, control its rectification condition and make the oxygen of the second oxygen-enriched liquid air
Content, less than the oxygen content of prior art, is such as 70～82%, and the second oxygen-enriched liquid air enters the evaporation side of condenser/evaporator and is positioned at
The nitrogen of condensation side carries out heat exchange (from lower rectifying column 81, concrete source sees below this nitrogen)；Another road air is empty through second
Letter shoot road 104 enters the vaporizer 91 of the 3rd rectifying column 90, in order to provide the rising needed for the 3rd rectifying column 90 rectification to steam
Vapour, and self carried out rectification by the lower rectifying column 81 of entrance after partial liquefaction；The air quilt of partial liquefaction in lower rectifying column 81
The first oxygen-enriched liquid air and top nitrogen is obtained after rectification；Top nitrogen is conveyed into condenser/evaporator 82 by nitrogen transfer pipeline 102
Condensation side, and heat the second oxygen-enriched liquid air of the evaporation side of this condenser/evaporator 82, and self be condensed rear portion as under
The backflow of rectifying column 81, another part liquid nitrogen goes rectifying column 83 rectification.Rich owing to being positioned at the second of this condenser/evaporator 82
The oxygen content of oxygen liquid air is low so that the evaporating temperature at condenser/evaporator 82 reduces, so that the condensation of condenser/evaporator 82
Temperature reduces, and then causes the pressure in lower rectifying column 81 to reduce, further such that the row pressure of compressor 20 reduces, and compresses
The row pressure of machine 20 reduces the most energy-conservation for realization.On the basis of achieving above-mentioned energy-saving effect, utilize the second oxygen-enriched liquid air
Relatively low the second oxygen-enriched liquid air being unsatisfactory for product demand of oxygen content that upper rectifying column 83 is produced by transfer pipeline 103 is conveyed into the 3rd essence
Evaporate tower 90 and carry out rectification, and then be met the oxygen enriched product of product demand.Simultaneously because, air compares nitrogen at the same pressure
Condensation temperature is high, and air goes out the state of vaporizer 91 gas-liquid two-phase simultaneously, the bubble point temperature of temperature condensation more complete than air under this state
Height, thus reach while compressor 20 pressure at expulsion reduces, it is ensured that the heat transfer temperature difference of vaporizer 91, meet the 3rd rectification
The upflowing vapor that tower 90 is required during rectification the second oxygen-enriched liquid air.
As can be seen here, the application is by controlling its rectification condition during rectifying column 83 in application, it is achieved that reduce compressor 20
Row pressure, and then achieve energy-conservation purpose；Meanwhile, the oxygen content utilizing the 3rd rectifying column 90 to produce upper rectifying column 83 is relatively low
The second oxygen-enriched liquid air carry out further rectification, obtained the oxygen enriched product that oxygen content is higher.The application is obtaining oxygen enriched product
Meanwhile, it is capable to produce nitrogen and partially liq product, product category is enriched, and improves production capacity benefit further.
In order to improve product extraction ratio, preferably as it is shown in figure 1, in the top of above-mentioned 3rd rectifying column 90 and upper rectifying column 83
Portion is connected by top gas transfer pipeline 105 and interface is positioned at below oxygen-enriched liquid air import.3rd rectifying column 90 top is produced
Fraction gas be delivered in rectifying column 83 to carry out continue rectification by top gas transfer pipeline 105.
In order to improve product extraction ratio, preferably as it is shown in figure 1, the bottom of above-mentioned lower rectifying column 81 and upper rectifying column 83 oxygen-enriched
Liquid air import is connected by the first oxygen enriched liquid transfer pipeline 106.Enter with the oxygen-enriched liquid air that the rectification of lower rectifying column 81 is obtained
One step rectification, the second oxygen-enriched liquid air produced in upper rectifying column 83 rectification enters the 3rd rectifying column 90 further rectification raising oxygen
Purity.
In order to improve the rectification efficiency of upper rectifying column 83, preferably as it is shown in figure 1, air separation equipment also includes subcooler 70, mistake
Cooler 70 is arranged on the first oxygen enriched liquid transfer pipeline 106.Utilize the first oxygen-rich liquid of subcooler rectifying column 83 upper to input
Sky carries out supercool.
In order to improve the rectification efficiency of upper rectifying column 83, the most above-mentioned condenser/evaporator 82 condensation side and the top of upper rectifying column 83
It is connected by liquid nitrogen transfer pipeline 107, and liquid nitrogen transfer pipeline 107 is arranged, with by rectifying column 83 in conveying through subcooler 70
Liquid nitrogen supercool.
In order to improve rectification efficiency, preferably enter the vaporizer 91 of the 3rd rectifying column 90 at air before, carry out heat exchange, preferably
As it is shown in figure 1, above-mentioned air separation equipment also includes that main heat exchanger 60, main heat exchanger 60 are arranged on the second air delivery pipe
On 104.
Product temperature obtained by the application rectification is relatively low, and its heat can be further with, preferably as it is shown in figure 1, upper rectification
Tower 83 top connects has product nitrogen gas output pipe 108, product nitrogen gas output pipe 108 to sequentially pass through subcooler 70 and main heat exchange
Device 60 is arranged.In utilization, the product nitrogen gas of rectifying column 83 output uses as the low-temperature receiver of subcooler 70 and main heat exchanger 60, and
Self is by re-heat.Based on above-mentioned it is also contemplated that, further preferably as it is shown in figure 1, connect bottom the 3rd rectifying column 90 and have oxygen rich air
Body product transfer pipeline 109, oxygen rich gas product transfer pipeline 109 is arranged through main heat exchanger 60.
Preferably as it is shown in figure 1, above-mentioned air separation equipment also includes that pre-cooling purification unit 30, the first air delivery pipe 101 depend on
Secondary connection compressor 20, pre-cooling purification unit 30, the middle part of upper rectifying column 83, the second air delivery pipe 104 is sequentially connected with
Compressor 20, pre-cooling purification unit 30 and air intake.The most above-mentioned first air delivery pipe 101 and the conveying of the second air
Pipeline 104 merges setting between the outlet and compressor 20 of pre-cooling purification unit 30.
The application is in order to improve the purification effect of air, preferably as it is shown in figure 1, above-mentioned pre-cooling purification unit 30 includes being sequentially connected
It is arranged on pre-cooler 31 and the purification devices 32 in compressor 20 downstream.Air is after pre-cooler 31, and moisture reduces,
Molecular sieve in Simultaneous purification device 32 is to CO2Dynamic adsorption capacity increase, it is ensured that the purification effect of air.
Additionally, in order to improve nitrogen product purity further, preferably as it is shown in figure 1, above-mentioned upper rectifying column 83 connects dirty nitrogen
Transfer pipeline 110, dirty nitrogen transfer pipeline 110 sequentially pass through subcooler 70 and main heat exchanger 60 and end respectively with pre-cooler
31 are connected with purification devices 32.Dirt nitrogen is delivered to pre-cooler 31 by dirty nitrogen transfer pipeline 110 and reclaims cold further
Amount.Enter the dirty nitrogen of purification devices 32 as regeneration source of the gas.
In the application preferred embodiment, preferably as it is shown in figure 1, above-mentioned air separation equipment also includes booster expansion machine 40 He
Cooler 50, booster expansion machine 40 has pressurized end 41 and expanding end 42, pressurized end 41 and expanding end 42 according to air flow
It is successively set on the first air delivery pipe 101, and is arranged on main heat exchanger 60 times along air-flow direction expanding end 42
Trip；Cooler 50 is arranged on the first air delivery pipe 101 and between pressurized end 41 and main heat exchanger 60.
Enter the pressurized end through booster expansion machine 40 after the air of the first air delivery pipe 101 is flowed out by pre-cooling purification unit 30
41 superchargings and through subcooler 50 cool down after, enter main heat exchanger 60 expansion gas passage, then taken out by the middle part of main heat exchanger 60
The expanding end 42 going out to enter booster expansion machine 40 expands, and enters upper rectifying column 83 after expansion.
Additionally, in order to protect compressor, the most above-mentioned air separation equipment also includes that air filter 10, air filter 10 set
Put the dust etc. filtering to remove in air to the air entering compressor 20 in the upstream of compressor 20 and may filter that impurity.
In the another kind of typical embodiment of the application, it is provided that a kind of air separating method, in the employing of this air separating method
The air separation equipment stated carries out air separation, wherein, utilize the double rectification column of air separation equipment upper rectifying column 83
To the second oxygen-enriched liquid air that oxygen content is 70～82%；Second oxygen-enriched liquid air obtains oxygen through the rectification of the 3rd rectifying column 90 and contains
The gas products of amount more than 90% and the fluid product of oxygen content more than 95%, this technical oxygen extraction ratio 97～99.5%.
Owing to above-mentioned air separating method can be utilized to lower oxygen content in the oxygen-enriched liquid air of upper rectifying column, and then pressure can be reduced
The row pressure of contracting machine, thus realize energy-conservation；The oxygen content simultaneously utilizing the 3rd rectifying column of increase to obtain upper rectifying column is relatively low
Oxygen-enriched liquid air carries out rectification, and then can be met the oxygen product of requirement.
In order to be more fully understood that the application, the air separation equipment shown in the application Fig. 1 how is utilized to enter by schematically illustrating below
Line space edema caused by disorder of QI from.
Air, after air filter 10 filtering and impurity removing, enters compressor 20 and is compressed to 0.315MPa, rear entrance pre-cooler 31,
Purification devices 32 carries out pre-cooling and purification successively, and the air pressure after purification is 0.3MPa, and flow is 101200Nm3/h。
Air after purification is divided into two-way, and pressurized end 41 supercharging of an intensified decompressor of road air 40 is the coldest through subcooler 50
But, after, the expansion gas passage of main heat exchanger 60 is entered, then by extracting the swollen of entrance booster expansion machine 40 in the middle part of main heat exchanger 60 out
Swollen end 42 expands, and enters upper rectifying column 83 after expansion.Another road air enters after main heat exchanger 60 is cooled to dew point temperature
The vaporizer 91 of three rectifying columns 90, provides upflowing vapor for the 3rd rectifying column 90, and self is entered lower rectifying column after partial liquefaction
81 carry out rectification.
Obtaining the second oxygen-enriched liquid air and top nitrogen that oxygen content is 81% in upper rectifying column 83, this second oxygen-enriched liquid air is the 3rd
Rectifying column 90 continues rectification, obtains the product oxygen of 90%.This product oxygen is sent as product through main heat exchanger 60 re-heat.
Upper rectifying column 83 top nitrogen is sent as pure nitrogen gas product after sequentially passing through subcooler 70 and main heat exchanger 60 re-heat, and yield is
50000Nm3/h；After the dirty nitrogen extracted out from the middle and upper part of upper rectifying column 83 sequentially passes through subcooler 70 and main heat exchanger 60 re-heat
Go pre-cooling purification unit 30.
In lower rectifying column 81, the air of partial liquefaction obtains the first oxygen-enriched liquid air and top nitrogen after being distillated, and top nitrogen is passed through
Nitrogen transfer pipeline 102 is conveyed into the condensation side of condenser/evaporator 82, and heat this condenser/evaporator 82 evaporation side second
Oxygen-enriched liquid air, and the rear section backflow as lower rectifying column 81 that self is condensed, another part liquid nitrogen and lower rectifying column 81 end
Portion's the first oxygen-enriched liquid air enters rectifying column 83 after subcooler 70 and carries out rectification.
Second oxygen-enriched liquid air of upper rectifying column 83 is conveyed into the 3rd rectifying column 90 and carries out essence by the second oxygen-enriched liquid air transfer pipeline 103
Evaporating, at oxygen product and the liquid oxygen product of 96% of acquisition 90% at the bottom of tower, wherein the yield of liquid oxygen product is 200Nm3/ h, oxygen
The yield of product is 23150Nm3/h。
As can be seen here, the compressor row pressure of above-mentioned technique is 0.315MPa, compared to tradition pure oxygen energy saving technology about 20%, compares
In two-tower rectification ultralow pressure oxygen enriching process saving energy 10%.
As can be seen from the above description, the above embodiments of the present invention achieve following technique effect:
The application is by controlling the rectification condition of upper rectifying column, it is achieved that reduces the row pressure of compressor, and then achieves energy-conservation mesh
's；Meanwhile, relatively low the second oxygen-enriched liquid air of the oxygen content that utilizes the 3rd rectifying column to produce upper rectifying column carries out further rectification,
Obtain the oxygen enriched product that oxygen content is higher.Meanwhile, the vaporizer thermal source in using air as the 3rd rectifying column, it is ensured that evaporation
Device heat transfer temperature difference under raw air lower pressure, provides rectification condition for the 3rd rectifying column.Further, the application is obtaining
While oxygen enriched product, it is possible to produce nitrogen and partially liq product, product category is enriched, and improves production capacity benefit further.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for those skilled in the art
For, the present invention can have various modifications and variations.All within the spirit and principles in the present invention, any amendment of being made, etc.
With replacement, improvement etc., should be included within the scope of the present invention.
Claims (11)
1. an air separation equipment, including:
Compressor (20)；
Double rectification column, described double rectification column includes rectifying column (83), lower rectifying column (81) and is arranged on described
Condenser/evaporator (82) between rectifying column (83) and lower rectifying column (81), the middle part tool of described upper rectifying column (83)
Oxygen-enriched liquid air import, described compressor (20) is had to pass through the first air delivery pipe with the middle part of described upper rectifying column (83)
Road (101) is connected and interface is positioned at below described oxygen-enriched liquid air import, and the top of described lower rectifying column (81) is cold with described
Solidifying vaporizer (82) is connected by nitrogen transfer pipeline (102) so that nitrogen enters the cold of described condenser/evaporator (82)
Second oxygen-enriched liquid air of evaporation side of described condenser/evaporator (82) is also heated in solidifying side, and described second oxygen-enriched liquid air is from institute
Stating rectifying column (83), described nitrogen is from described lower rectifying column (81), it is characterised in that described air separation equipment
Also include:
3rd rectifying column (90), passes through the second oxygen-enriched liquid air transfer pipeline (103) with the bottom of described upper rectifying column (83)
It is connected and the second oxygen-enriched liquid air that described upper rectifying column (83) produces is delivered to described 3rd rectifying column (90) carries out rectification,
The bottom of described 3rd rectifying column (90) is provided with vaporizer (91), and described vaporizer (91) has air intake and sky
Gas exports, and described air intake is connected by the second air delivery pipe (104) with described compressor (20), described sky
Gas outlet is connected with described lower rectifying column (81).
Air separation equipment the most according to claim 1, it is characterised in that the top of described 3rd rectifying column (90) and institute
State the middle part of rectifying column (83) by top gas transfer pipeline (105) is connected and interface is positioned at described oxygen-enriched liquid air and enters
Below Kou.
Air separation equipment the most according to claim 1, it is characterised in that the bottom of described lower rectifying column (81) is with described
The oxygen-enriched liquid air import of upper rectifying column (83) is connected by the first oxygen enriched liquid transfer pipeline (106).
Air separation equipment the most according to claim 3, it is characterised in that described air separation equipment also includes:
Subcooler (70), is arranged on described first oxygen enriched liquid transfer pipeline (106).
Air separation equipment the most according to claim 4, it is characterised in that described condenser/evaporator (82) condensation side and institute
The top stating rectifying column (83) is connected by liquid nitrogen transfer pipeline (107), and described liquid nitrogen transfer pipeline (107)
Arrange through described subcooler (70).
Air separation equipment the most according to claim 4, it is characterised in that described air separation equipment also includes:
Main heat exchanger (60), is arranged on described second air delivery pipe (104).
Air separation equipment the most according to claim 6, it is characterised in that described upper rectifying column (83) top connects product
Product nitrogen output pipe (108), described product nitrogen gas output pipe (108) sequentially passes through described subcooler (70) and institute
State main heat exchanger (60) to arrange.
Air separation equipment the most according to claim 6, it is characterised in that described 3rd rectifying column (90) bottom connects to be had
Oxygen rich gas product transfer pipeline (109), described oxygen rich gas product transfer pipeline (109) passes described main heat exchanger (60)
Arrange.
Air separation equipment the most according to claim 6, it is characterised in that described air separation equipment also includes:
Pre-cooling purification unit (30), described first air delivery pipe (101) is sequentially connected with described compressor (20), institute
Stating pre-cooling purification unit (30), the middle part of described upper rectifying column (83), described second air delivery pipe (104) depends on
The described compressor of secondary connection (20), described pre-cooling purification unit (30) and described air intake, described first air conveying
Pipeline (101) and described second air delivery pipe (104) in the outlet of described pre-cooling purification unit (30) with described
Merge between compressor (20) and arrange.
Air separation equipment the most according to claim 9, it is characterised in that described air separation equipment also includes:
Booster expansion machine (40), has pressurized end (41) and an expanding end (42), described pressurized end (41) and described swollen
Swollen end (42) is successively set on described first air delivery pipe (101) according to air flow, and according to described air
Flow to described expanding end (42) and be arranged on the downstream of described main heat exchanger (60)；
Cooler (50), be arranged on described first air delivery pipe (101) upper and be positioned at described pressurized end (41) with
Between described main heat exchanger (60).
11. 1 kinds of air separating methods, it is characterised in that use the air separation equipment according to any one of claim 1 to 10 to enter
Line space edema caused by disorder of QI from, wherein, utilize the double rectification column of described air separation equipment upper rectifying column (83) obtain oxygen
Content is the second oxygen-enriched liquid air of 70～82%；Described second oxygen-enriched liquid air obtains through the rectification of described 3rd rectifying column (90)
Gas products and the fluid product of oxygen content more than 95% to oxygen content more than 90%.
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| CN201610392029.8A CN105910388A (en) | 2016-06-03 | 2016-06-03 | Air separation device and air separation method |
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| CN201610392029.8A CN105910388A (en) | 2016-06-03 | 2016-06-03 | Air separation device and air separation method |
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| CN106958988A (en) * | 2017-04-19 | 2017-07-18 | 苏州市兴鲁空分设备科技发展有限公司 | The device for making of oxygen rich air |
| CN109028760A (en) * | 2018-08-29 | 2018-12-18 | 开封黄河空分集团有限公司 | Air-separating plant |
| CN111542724A (en) * | 2017-11-29 | 2020-08-14 | 乔治洛德方法研究和开发液化空气有限公司 | Method and apparatus for separating air by cryogenic distillation |
| CN114130153A (en) * | 2021-11-20 | 2022-03-04 | 开封黄河空分集团有限公司 | Air separation device and method for preparing large liquid amount |
| CN114485055A (en) * | 2022-02-11 | 2022-05-13 | 开封黄河空分集团有限公司 | Air cryogenic cooling liquefaction method for air separation |
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| CN114130153A (en) * | 2021-11-20 | 2022-03-04 | 开封黄河空分集团有限公司 | Air separation device and method for preparing large liquid amount |
| CN114485055A (en) * | 2022-02-11 | 2022-05-13 | 开封黄河空分集团有限公司 | Air cryogenic cooling liquefaction method for air separation |
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Application publication date: 20160831 |