CN1168464A - Air separating method and equipment - Google Patents
Air separating method and equipment Download PDFInfo
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- CN1168464A CN1168464A CN 96116391 CN96116391A CN1168464A CN 1168464 A CN1168464 A CN 1168464A CN 96116391 CN96116391 CN 96116391 CN 96116391 A CN96116391 A CN 96116391A CN 1168464 A CN1168464 A CN 1168464A
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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
- F25J3/044—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 single pressure main column system only
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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
- F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
- F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another 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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04278—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using external refrigeration units, e.g. closed mechanical or regenerative refrigeration units
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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
- F25J3/04309—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 nitrogen
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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
- F25J3/0466—Producing crude argon in a crude argon column as a parallel working rectification column or auxiliary column system in a single pressure main column system
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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
- 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
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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
- F25J2200/52—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the high pressure column of a double pressure main column system
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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
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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
- F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/42—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being nitrogen
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
Abstract
The present invention is oxygen, nitrogen and argon preparing method and equipment through low-temp rectification of air. It can prepare in single-stage rectifying equipment and at the condition of very low power consumption pure nitrogen product with 3 ppm-5% oxygen content and oxygen-riched or pure oxygen product with 60-99.5% oxygen content. It can prepared in two-stage rectifying equipment pure oxygen product with 99.5-99.999% oxygen content and pure nitrogen product with 3 ppm-2% oxygen content. It may prepare argon by setting a crude argon tower near pressure tower or low pressure tower. It has extremely high extraction rate of oxygen, nitrogen and argon.
Description
The invention belongs to the field of cryogenic rectification air separation, the principle separation of air of application of cold temperature rectifying is produced the method and apparatus of oxygen, nitrogen, argon gas.
Traditional single rectification column flow process generally only can be produced single oxygen enrichment or pure nitrogen gas, and the product recovery rate is low, if will produce more products gas, must pass through to increase the method for pressure, and technology stream complexity.Corresponding energy consumption is also higher.Traditional double rectification column flow process, column plate is many, and volume is big, and energy consumption is high could produce pure oxygen and low-pressure nitrogen.
In view of above-mentioned technique known deficiency, task of the present invention is to propose a kind of improved air separating method and equipment, it is under lower energy consumption condition, produce by the single-stage rectifying device that to contain oxygen be 5%～3ppm nitrogen product, can also produce that to contain oxygen be 70～99.5% oxygen enrichment or pure oxygen product, perhaps produce the oxygen product that contains oxygen 99.5%～99.999% and contain the pressure purity nitrogen product that oxygen is 2%～3ppm by the twin-stage rectifying device.Set up a crude argon column at pressure column or lower pressure column and get argon gas.To oxygen, nitrogen, argon gas all has high recovery rate.
Task of the present invention solves with following method: a kind of air separating method of single rectification column, it is characterized in that an evaporimeter being set in the pressure column bottom, a condenser is set at the pressure column top or in pressure column, also is provided with the auxiliary condenser group, enter after the compressed raw air cooling and remove moisture content in the molecular sieve adsorber, carbon dioxide, acetylene and other hydrocarbon partials form and purify raw air, enter by the cooled raw air of main heat exchanger in the evaporimeter of pressure column bottom and make heating source of the gas heating liquid air, after being cooled, raw air goes out evaporimeter, after in subcooler, being cooled to condensing temperature again, entering the pressure column middle part and carry out the rectifying separation; The condenser that is provided with at the pressure column top or uprising gas in the auxiliary condenser group condensing tower is set in pressure column again, oxygen enrichment of being drawn by the pressure column bottom or pure oxygen liquid enter the low-temperature receiver that the overhead condenser low-pressure side is made tower after subcooler is crossed cold decompression cooling.Oxygen in the tower in the uprising gas is according to the rectifying equilibrium principle in the tower, successively be condensed at auxiliary condenser and overhead condenser, and form enough phegmas, and carry out rectifying with uprising gas with being arranged on column plate in the tower or the filler, oxygen in the uprising gas is condensed, and can obtain high-purity liquid nitrogen at cat head at last.Can obtain oxygen enrichment or pure oxygen liquid in overhead condenser, the pressure differential by regulating condenser two sides is to obtain enough condensation temperature difference.
The expanding gas that feeds low temperature in auxiliary condenser is made the low-temperature receiver of tower.
A kind of air separating method of cryogenic rectification, it is the flow process that adopts double rectification column, it is based on pressure column, by entering the low-temperature receiver that lower pressure column top condenser low-pressure side is made lower pressure column after the pure liquid nitrogen decompression cooling that pressure column obtained, pressure cat head condenser/evaporator is as the thermal source of lower pressure column, rectifying separates oxygen enrichment or the pure oxygen liquid air from the pressure column still, is that portion can obtain pure oxygen at the bottom of lower pressure column.
In tower, be equipped with column plate section or filler.
Air separation equipment flow process of the present invention is divided gas flow pressuring expansion flow process or the expansion flow process that supercharger is not set.Band after promptly rectifying separates in pressure column is pressed nitrogen, enter decompressor to the uniform temperature in the heat exchanger package re-heat and make adiabatic expansion, enter in the auxiliary condenser set in the rectifying column again and make low-temperature receiver, perhaps re-heat in subcooler goes out device then after the heat exchanger package re-heat.
In order to produce high purity nitrogen product and purity oxygen simultaneously, must have the ability of separating crude argon at Dan Tazhong, the extraction of crude argon can improve the rectifying operating mode of rectifying column, and the set crude argon flow process of the present invention is to be purpose to produce high purity nitrogen product, to produce purity oxygen simultaneously.
Task of the present invention solves with following air separation equipment.
A kind of air separation equipment flow process of single rectification column is characterized by:
A. compressed raw air is removed moisture content, carbon dioxide, acetylene and other part hydrocarbons and is formed the purification raw air in molecular sieve adsorber.
B. after purifying raw air and entering main heat exchanger, entered the liquia air in the heating kettle in the evaporimeter of rectifier bottoms after the gas cooled of backflowing, in subcooler, entered the rectifying column middle part again after the cooling.
C. the rectifying column top is provided with a condenser and is provided with the auxiliary condenser group in rectifying column, pressure oxygen enrichment of drawing from rectifier bottoms or pure oxygen liquid subcooler, cross cold after, after the decompression cooling, enter the low-temperature receiver of making tower in the overhead condenser again, gas after being heated is made product gas again after the heat exchanger package re-heat.
D. the pressure pure nitrogen gas of drawing from the pressure column top is made product gas in the main heat exchanger re-heat to normal temperature.And enter decompressor at main heat exchanger middle part extension pressure nitrogen gas and make adiabatic expansion.For the sky branch flow process that adopts pressuring expansion, pressure nitrogen gas after the main heat exchanger re-heat then enters in the supercharger of decompressor after the supercharging, enter again to be cooled in the main heat exchanger and enter decompressor after the uniform temperature again and make adiabatic expansion, expanding gas then enters in the set auxiliary condenser of the interior suitable position of rectifying column and makes low-temperature receiver, go out to go out device through the main heat exchanger re-heat again behind the heat exchanger and make product gas, a part of gas enters molecular sieve adsorber and makes heated air.
E. the pure liquid nitrogen product of part can be obtained from the pressure column top, part liquid oxygen product can be obtained from the overhead condenser low-pressure side.
A kind of air separation equipment flow process of single rectification column is characterized by:
A. compressed raw air is removed moisture content, carbon dioxide, acetylene and other hydrocarbon partials and is formed the purification raw air in molecular sieve adsorber.
B. after purifying raw air and entering main heat exchanger, entered the liquia air in heating tower's still in the evaporimeter of rectifier bottoms after the gas cooled of backflowing, in subcooler, entered the rectifying column middle part again after the cooling.
C. the rectifying column top is provided with a condenser, pressure oxygen enrichment of drawing from rectifier bottoms or pure oxygen liquid subcooler, cross cold after, after the decompression cooling, enter the low-temperature receiver that the condenser low-pressure side is made tower again.
D. after entering the subcooler heat exchange from the oxygen enrichment of the condenser low-pressure side at rectifying column top evaporation or pure oxygen gas, again after the heat exchanger package re-heat ejector as product gas.The pure liquid nitrogen product of part can be obtained from the pressure column top, part liquid oxygen product can be obtained from the condenser low-pressure side.
E. the pressure pure nitrogen gas of drawing from the rectifying column condenser enters decompressor in the heat exchanger package re-heat to the uniform temperature and makes adiabatic expansion.For the sky branch flow process that adopts pressuring expansion, pressed gas after the main heat exchanger re-heat then enters in the supercharger of decompressor after the supercharging, enter again to be cooled in the main heat exchanger to enter again after the uniform temperature and make adiabatic expansion in the decompressor, expanding gas then enters in the subcooler after the re-heat, go out to go out device through the main heat exchanger re-heat again behind the subcooler and make product gas, a part of gas enters molecular sieve adsorber and makes heated air.
Rectifying column is a pressure column, and has the air separation equipment flow process of Cryo Gas Refrigerator, it is characterized by:
A. compressed raw air is removed moisture content, carbon dioxide, acetylene and other hydrocarbon partials and is formed the purification raw air in molecular sieve adsorber.
B. after purifying raw air and entering the gas cooled of being backflowed behind the main heat exchanger, enter heating liquid air in the evaporimeter of pressure column bottom.
C. pressure column bottom is provided with an evaporimeter, enters the purification raw air of making thermal source in the evaporimeter and goes out evaporimeter after by the liquia air cooling, enters a subcooler again and is backflowed after the gas cooled liquefaction, enters the pressure column middle part.
D. the pressure column top pressure nitrogen gas of drawing enters the low-temperature receiver that reenters tower in the pressure column evaporator overhead condenser that is liquefied in the Cryo Gas Refrigerator, nitrogen after the evaporation is made product gas after subcooler and main heat exchanger re-heat, wherein a part enters molecular sieve adsorber and makes regeneration gas.
E. from pressure column bottom or column plate oxygen rich gas ejector after the main heat exchanger re-heat of drawing make product gas.A part of pure liquid product can be obtained from the pressure column evaporator overhead condenser, the empty product of rich solution can be obtained from the pressure column bottom.
A kind of air separation equipment of double rectification column is set up the air separating technological of a crude argon column, it is characterized by:
A. compressed raw air is removed moisture content, carbon dioxide, acetylene and other hydrocarbon partials and is formed the purification raw air in molecular sieve adsorber.
B. after purifying raw air and entering main heat exchanger cooling, enter the liquia air in heating tower's still in the evaporimeter of pressure column bottom again.
C. the pressure column bottom is provided with an evaporimeter, enters to go out evaporimeter after the pressure raw air of making thermal source in the evaporimeter is cooled off by liquia air, enters a heat exchanger again and is backflowed gas cooled after condensing temperature, and the pressure raw air enters the pressure column middle part.
D. the pressure column top is provided with a condenser/evaporator, and a part of pure liquid nitrogen that is condensed by the pressure column top enters the low-temperature receiver that low pressure overhead condenser low-pressure side is made lower pressure column after a pressure-reducing valve cooling, and the pure liquid nitrogen of another part is made the phegma of pressure column.
E. the oxygen enriched liquid air of being drawn from pressure column bottom, through the gas that backflows that a subcooler is gone out tower cross cold after, after a decompression decompression cooling, enter the lower pressure column middle part again and carry out rectifying once more.
F. the low-pressure nitrogen that is evaporated from the lower pressure column evaporator overhead condenser enters the heat exchanger package re-heat again and make product gas to normal temperature after a subcooler re-heat.
Nitrogen ejector after the heat exchanger package re-heat of g. being drawn from the pressure column top is made purity nitrogen product gas, obtains pure liquid product in the condenser of lower pressure column bottom; Draw high purity oxygen gas on condenser top at the bottom of the lower pressure column and to normal temperature, make product gas through the heat exchanger package re-heat; Can obtain pure liquid nitrogen product in lower pressure column evaporator overhead condenser gas nitrogen side and pressure column top.
H. the pressure nitrogen gas part after from re-heat to uniform temperature enters and makes the expansion source of the gas the decompressor, expanding gas then enters in the interior auxiliary condenser of pressure column by after the re-heat, after perhaps expanding gas directly enters a subcooler, make product gas again in main heat exchanger after the re-heat, wherein a part of nitrogen enters and makes heated air in the molecular sieve adsorber.
I. the crude argon column top is provided with a condenser, introduce pressure column condensed oxygen enrichment in bottom or pure oxygen liquid, after crossing cold decompression, subcooler enters the low-temperature receiver of making tower in the crude argon column condenser, by the set column plate section argon enrichment region in bottom, lower pressure column oxygen enriched liquid porch, drawing a part of argon fraction gas enters the crude argon column bottom and makes unstripped gas, in tower after the rectifying, discharge small amount of exhaust gas in the crude argon overhead condenser, the liquid of crude argon column bottom still returns into the lower pressure column corresponding site, crude argon then draws at the crude argon column top, and the oxygen rich air of being evaporated in the condenser is still returned in the lower pressure column.
Pressure column is set up the air separation equipment flow process of a crude argon column, its feature:
A. the crude argon column top is provided with a condenser, and the condensation liquid oxygen of introducing rectifier bottoms enters the low-temperature receiver that condenser is made tower after lowering the temperature through cold decompression.
B. pressure column purifies the set column plate section middle part argon fraction enrichment region in bottom, raw air porch and draws a part of argon fraction gas and enter the crude argon column bottom and make unstripped gas.
C. after the rectifying, the phegma that is obtained at the bottom of tower still returns into the pressure column corresponding site unstripped gas in crude argon column.
D. liquid oxygen is evaporated in the condenser that enters the crude argon column top, and evaporation oxygen still returns out in the low oxygen pipeline that rectifying column top condenser evaporated.
E. unstripped gas after the rectifying, is discharged small amount of exhaust gas in overhead condenser in crude argon column, and crude argon is then drawn at the crude argon column top.
Below in conjunction with flow chart, various air separation equipment flow processs are described.
The air separation equipment flow process of a kind of single rectification column of Fig. 1.
The air separation equipment flow process of a kind of single rectification column of Fig. 2.
A kind of air separation equipment flow process that has Cryo Gas Refrigerator of Fig. 3.
A kind of double rectification column of Fig. 4 is set up the air separation equipment flow process of crude argon column.
A kind of double rectification column of Fig. 5 is set up the air separation equipment flow process of crude argon column.
Fig. 6 rectifying column is set up the air separation equipment flow process of a crude argon column.
Fig. 1 is that rectifying column is the air separation equipment flow process of a rectifying column.After raw air enters compressor 2 compression cooling drainings by pipeline 1, enter molecular sieve adsorber 4 by pipeline 3 and remove moisture content, carbon dioxide, acetylene and other hydrocarbons, after pipeline 5, main heat exchanger 6 are backflowed gas cooled, enter in the rectifying column 10 bottom evaporimeters 8 through pipeline 7 and to make heated air, drawn by pipeline 12 by the cooled pressure raw air of oxygen-enriched liquid air, after entering subcooler 13 and being cooled to condensing temperature, enter rectifying column 10 middle parts through pipeline 14.Rectifying column 10 tops are provided with condenser 11 and the Ta Nei suitable position is provided with an auxiliary condenser 47, uprising gas is successively by 11 condensations of the condenser of auxiliary condenser 47 and cat head in the tower, produce enough phegmas in tower, by pipeline 55, valve 56 can obtain the partially liq product.
Draw at the tower still and to contain oxygen and enter subcooler 13 and 18 through pipeline 26 greater than 60% pressure oxygen enriched liquid, cross cold after, through pipeline 27, pressure-reducing valve 28 decompression cooling backs are entered in the tower condenser 11 by pipeline 29 makes low-temperature receiver.Boil-off gas is drawn by pipeline 30 again, in the subcooler 18 and 13 and after main heat exchanger 6 re-heats, draw at pipeline 32 and to make product oxygen, draw through cooler 18 and 13 by pipeline 22, make pressure pure nitrogen gas product after main heat exchanger 6 re-heats by the pressure nitrogen that draw at pressure column 10 tops.Undertaken in the booster 41 after the supercharging by pipeline 40 to the normal temperature in main heat exchanger 6 re-heats, after pipeline 42 enters main heat exchanger 6 to be cooled to uniform temperature, enter in the decompressor 44 and make adiabatic expansion by pipeline 43, expanding gas is drawn by pipeline 46, enter the low-temperature receiver of making tower in the auxiliary condenser 47 again, or the pressure nitrogen gas of drawing from main heat exchanger 6 middle parts directly enters decompressor 44 and makes expanding gas.Go out gas behind the tower again through pipeline 48, enter subcooler 13 and 6 re-heats of main parallel operation are made product gas to normal temperature, wherein a part of nitrogen advances molecular sieve adsorber 4 by pipeline 51 and makes regeneration gas, again by pipeline 52 emptying.
Fig. 2 is that rectifying column is the air separation equipment flow process of a pressure column.
Compared to Figure 1 difference is that auxiliary condenser is not set in the tower, and from the pipeline 22 impulse power pure nitrogen gas at rectifying column 10 tops product gas and make expanding gas after re-heat, expanding gas is made product gas through pipeline 46 after subcooler 13 and main heat exchanger 6 re-heats.
A kind of air separation equipment flow process that has Cryo Gas Refrigerator of Fig. 3.
Compare with Fig. 2, the cancellation expander system, be increased in pressure column 10 tops draw a pressure nitrogen gas enter be liquefied in the Cryo Gas Refrigerator 25 after, enter overhead condenser through pipeline 26 and make low-temperature receiver liquid, go out device after the boil-off gas re-heat.
A kind of double rectification column of Fig. 4 is set up crude argon column air separation equipment flow process.
After raw air enters compressor 2 compression cooling drainings by pipeline 1, enter molecular sieve adsorber 4 by pipeline 3 and remove moisture content, carbon dioxide, acetylene and other hydrocarbon partials, after pipeline 5 enters main heat exchanger 6 coolings, in pipeline 7 enters pressure column 10 evaporimeters 12, oxygen enriched liquid air in heating tower's still, raw air be cooled the back by pipeline 12 enter be cooled in the heat exchanger 13 reach condensing temperature after, enter pressure column 10 middle parts again through pipeline 14 again.Obtain to contain oxygen at the tower still and draw by pipeline 16 greater than 70% oxygen enrichment or pure oxygen liquid, by pipeline 24 enter subcooler 13 backflowed gas cross cold after, through pipeline 17, pressure-reducing valve 18 decompression backs enter lower pressure column 20 middle parts by pipeline 19.Uprising gas is by overhead condenser 15 condensations in the pressure column 10, the liquid of condensation is made the phegma of pressure column, by the pure condenser of a part of 15 condensations of condenser through pipeline 21, after pressure-reducing valve 23 reduces pressure to and is not less than 120KPa pressure, make the low-temperature receiver of lower pressure column 20 evaporator overhead condensers 25 through pipeline 24, must guarantee that condenser 25 2 sides have certain pressure differential to obtain the required condensation temperature difference, the liquid oxygen of condenser 15 low-pressure sides is evaporated, the gas nitrogen that lower pressure column 20 top condensers 25 are evaporated is drawn via pipeline 50, through subcooler 13, main heat exchanger 6 re-heats are to normal temperature, are drawn by pipeline 52 and make product gas.Small amount of exhaust gas is drawn through pipeline 55 in lower pressure column 25 tops, through heat exchanger 13, and main heat exchanger 6 re-heats emptying to the normal temperature.Obtaining nitrogenous pure nitrogen gas at 3ppm～99.999% at pressure column 10 tops is drawn by pipeline 33, at subcooler 13, main heat exchanger 6 re-heats are to normal temperature, obtain the pressure nitrogen gas product by pipeline 36 and go out device, containing oxygen is that 99.5～99.999% pure oxygens are through pipeline 30, subcooler 13, main heat exchanger 6 re-heats to normal temperature goes out device, draws product oxygen by pipeline 32.Pressure nitrogen gas after from the heat exchanger package re-heat to uniform temperature is drawn by pipeline 43 and is entered decompressor 44 and make adiabatic expansion, the expanding gas of drawing from pipeline 45 is again through subcooler 13, draw by pipeline 47 after main heat exchanger 6 re-heats and do product gas or emptying, draw a part of low-pressure nitrogen by pipeline 48 and enter molecular sieve adsorber and make regeneration gas, again by pipeline 49 emptying.Draw small amount of exhaust gas, emptying after the heat exchanger package re-heat from lower pressure column 20 top ducts 55.
A kind of double rectification column of Fig. 5 is set up crude argon column air separation equipment flow process.
Compare with Fig. 4, difference is that the gas after expanding enters in the auxiliary condensers set in the pressure column 10 44 by after the re-heat, makes product gas again after the heat exchanger package re-heat.
Fig. 6 is the air separation equipment flow process that pressure column has a crude argon column.
Comparing its change part with Fig. 2 is to increase the crude argon system flow, is described below:
In the stream of crude argon column, crude argon column 60 tops are provided with a condenser 61, and the argon enrichment region is drawn one argon fraction gas from the set column plate section 10a in raw air inlet duct 14 bottoms of rectifying column 10.Enter crude argon column 60 bottoms through pipeline 62, after oxygen in the uprising gas is condensed, its phegma still return pipe road is gone into for 63 times in the rectifying column 10, a part of liquid oxygen of being drawn from pressure-reducing valve 65 decompression backs, in entering crude argon column condenser 61, pipeline 66 makes the low-temperature receiver of tower, the gas that is evaporated is gone into for 67 times in the pipeline 30 by pipeline, discharge small amount of exhaust gas by valve 68 in crude argon column 60 evaporator overhead condensers 61, crude argon is then drawn from crude argon column 60 top ducts 69, micro amount of oxygen, the nitrogen further removed in the crude argon promptly obtain straight argon, and this exceeds scope involved in the present invention.This figure only relates to the relevant stream with rectifying column of crude argon column is set.
Claims (10)
1, a kind of air separating method of cryogenic rectification, enter after the compressed raw air cooling and remove moisture content in the molecular sieve adsorber, carbon dioxide, acetylene and other hydrocarbon partials form and purify raw air, and be cooled to condensing temperature by heat exchanger package, enter pressure column then and carry out the rectifying separation, it is characterized in that an evaporimeter being set in the pressure column bottom, and the feeding heated air is made the thermal source of tower, at the pressure column top condenser is set or also is provided with the auxiliary condenser group steam that rises in condensing tower in pressure column, the purification raw air that is cooled is introduced the middle part of rectifying column.
For the air separation equipment of double rectification column, it is characterized in that pressure column top is provided with a lower pressure column, and a condenser is set at the lower pressure column top, the condenser/evaporator at pressure column top is as the thermal source of lower pressure column, the oxygen rich gas in the rectifying lower pressure column.
Be equipped with column plate section or filler in the rectifying column.
2, single rectification column air separating method according to claim 1 is after the raw air that it is characterized in that feeding pressure column bottom evaporimeter is cooled, again through entering the pressure column middle part after the subcooler cooling liquid.Pressure oxygen enrichment of being drawn by the pressure column still or pure oxygen liquid enter after cooling, decompression cooling and make low-temperature receiver in the overhead condenser.
For the air separation equipment of double rectification column, it is characterized in that drawing pure liquid nitrogen that pressure column is condensed after the decompression cooling, the condenser low-pressure side that enters the lower pressure column top becomes to do the low-temperature receiver of lower pressure column, pressure column top condenser/evaporator is as the thermal source of lower pressure column, and rectifying separates the oxygen enriched liquid from the pressure column still.
3, according to claim 1,2 described single rectification column air separating methods, the cryogenic gas after it is characterized in that expanding enters in the auxiliary condenser of suitable position in the pressure column and makes low-temperature receiver, in tower after the re-heat, again through the heat exchanger package re-heat to normal temperature.
4, according to claim 1,2 described single rectification column air separating methods, it is characterized in that the derivative low-temperature pressure nitrogen of pressure cat head, enter and enter the low-temperature receiver that the pressure column evaporator overhead condenser is made tower after being liquefied in the Cryo Gas Refrigerator.
5, according to claim 1,2 described air separating methods, the argon fraction enrichment region that it is characterized in that the column plate section that pressure column purification bottom, raw air porch is set is drawn a part of argon fraction gas, perhaps draw a part of argon fraction gas at the suitable position of lower pressure column oxygen enriched liquid entrance bottom, feed the crude argon column bottom and make unstripped gas, the condensation liquid oxygen that feeds the rectifying column top in the condenser that the crude argon column top is provided with is made low-temperature receiver, uprising gas in the condensation crude argon column, crude argon is then drawn at the crude argon cat head, and condensed fluid still returns into corresponding site in pressure column or the lower pressure column.
6, a kind of air separation equipment flow process of single rectification column is characterized by:
A. compressed raw air is removed moisture content, carbon dioxide, acetylene and other part hydrocarbons and is formed the purification raw air in molecular sieve adsorber.
B. after purifying raw air and entering main heat exchanger, entered the liquia air in the heating kettle in the evaporimeter of rectifier bottoms after the gas cooled of backflowing, in subcooler, entered the rectifying column middle part again after the cooling.
C. the rectifying column top is provided with a condenser and is provided with the auxiliary condenser group in rectifying column, pressure oxygen enrichment of drawing from rectifier bottoms or pure oxygen liquid subcooler, cross cold after, after the decompression cooling, enter the low-temperature receiver of making tower in the overhead condenser again, gas after being heated is made product gas again after the heat exchanger package re-heat.
D. the pressure pure nitrogen gas of drawing from the pressure column top is made product gas in the main heat exchanger re-heat to normal temperature.And enter decompressor at main heat exchanger middle part extension pressure nitrogen gas and make adiabatic expansion.For the sky branch flow process that adopts pressuring expansion, pressure nitrogen gas after the main heat exchanger re-heat then enters in the supercharger of decompressor after the supercharging, enter again to be cooled in the main heat exchanger and enter decompressor after the uniform temperature again and make adiabatic expansion, expanding gas then enters in the set auxiliary condenser of the interior suitable position of rectifying column and makes low-temperature receiver, go out to go out device through the main heat exchanger re-heat again behind the heat exchanger and make product gas, a part of gas enters molecular sieve adsorber and makes heated air.
E. the pure liquid nitrogen product of part can be obtained from the pressure column top, part liquid oxygen product can be obtained from the overhead condenser low-pressure side.
7, a kind of air separation equipment flow process of single rectification column is characterized by:
A. compressed raw air is removed moisture content, carbon dioxide, acetylene and other hydrocarbon partials and is formed the purification raw air in molecular sieve adsorber.
B. after purifying raw air and entering main heat exchanger, entered the liquia air in heating tower's still in the evaporimeter of rectifier bottoms after the gas cooled of backflowing, in subcooler, entered the rectifying column middle part again after the cooling.
C. the rectifying column top is provided with a condenser, pressure oxygen enrichment of drawing from rectifier bottoms or pure oxygen liquid subcooler, cross cold after, after the decompression cooling, enter the low-temperature receiver that the condenser low-pressure side is made tower again.
D. after entering the subcooler heat exchange from the oxygen enrichment of the condenser low-pressure side at rectifying column top evaporation or pure oxygen gas, again after the heat exchanger package re-heat ejector as product gas.The pure liquid nitrogen product of part can be obtained from the pressure column top, part liquid oxygen product can be obtained from the condenser low-pressure side.
E. the pressure pure nitrogen gas of drawing from the rectifying column condenser enters decompressor in the heat exchanger package re-heat to the uniform temperature and makes adiabatic expansion.For the sky branch flow process that adopts pressuring expansion, pressed gas after the main heat exchanger re-heat then enters in the supercharger of decompressor after the supercharging, enter again to be cooled in the main heat exchanger to enter again after the uniform temperature and make adiabatic expansion in the decompressor, expanding gas then enters in the subcooler after the re-heat, go out to go out device through the main heat exchanger re-heat again behind the subcooler and make product gas, a part of gas enters molecular sieve adsorber and makes heated air.
8, rectifying column is a pressure column, and has the air separation equipment flow process of Cryo Gas Refrigerator, it is characterized by:
A. compressed raw air is removed moisture content, carbon dioxide, acetylene and other hydrocarbon partials and is formed the purification raw air in molecular sieve adsorber.
B. after purifying raw air and entering the gas cooled of being backflowed behind the main heat exchanger, enter heating liquid air in the evaporimeter of pressure column bottom.
C. pressure column bottom is provided with an evaporimeter, enters the purification raw air of making thermal source in the evaporimeter and goes out evaporimeter after by the liquia air cooling, enters a subcooler again and is backflowed after the gas cooled liquefaction, enters the pressure column middle part.
D. the pressure column top pressure nitrogen gas of drawing enters the low-temperature receiver that reenters tower in the pressure column evaporator overhead condenser that is liquefied in the Cryo Gas Refrigerator, nitrogen after the evaporation is made product gas after subcooler and main heat exchanger re-heat, wherein a part enters molecular sieve adsorber and makes regeneration gas.
E. from pressure column bottom or column plate oxygen rich gas ejector after the main heat exchanger re-heat of drawing make product gas.A part of pure liquid product can be obtained from the pressure column evaporator overhead condenser, the empty product of rich solution can be obtained from the pressure column bottom.
9, a kind of air separation equipment of double rectification column is set up the air separating technological of a crude argon column, it is characterized by:
A. compressed raw air is removed moisture content, carbon dioxide, acetylene and other hydrocarbon partials and is formed the purification raw air in molecular sieve adsorber.
B. after purifying raw air and entering main heat exchanger cooling, enter the liquia air in heating tower's still in the evaporimeter of pressure column bottom again.
C. the pressure column bottom is provided with an evaporimeter, enters to go out evaporimeter after the pressure raw air of making thermal source in the evaporimeter is cooled off by liquia air, enters a heat exchanger again and is backflowed gas cooled after condensing temperature, and the pressure raw air enters the pressure column middle part.
D. the pressure column top is provided with a condenser/evaporator, and a part of pure liquid nitrogen that is condensed by the pressure column top enters the low-temperature receiver that low pressure overhead condenser low-pressure side is made lower pressure column after a pressure-reducing valve cooling, and the pure liquid nitrogen of another part is made the phegma of pressure column.
E. the oxygen enriched liquid air of being drawn from pressure column bottom, through the gas that backflows that a subcooler is gone out tower cross cold after, after a pressure-reducing valve decompression cooling, enter the lower pressure column middle part again and carry out rectifying once more.
F. the low-pressure nitrogen that is evaporated from the lower pressure column evaporator overhead condenser enters the heat exchanger package re-heat again and make product gas to normal temperature after a subcooler re-heat.
Nitrogen ejector after the heat exchanger package re-heat of g. being drawn from the pressure column top is made purity nitrogen product gas, obtains pure liquid product in the condenser of lower pressure column bottom; Draw high purity oxygen gas on condenser top at the bottom of the lower pressure column and to normal temperature, make product gas through the heat exchanger package re-heat; Can obtain pure liquid nitrogen product in lower pressure column evaporator overhead condenser gas nitrogen side and pressure column top.
H. the pressure nitrogen gas part after from re-heat to uniform temperature enters and makes the expansion source of the gas the decompressor, expanding gas then enters in the interior auxiliary condenser of pressure column by after the re-heat, after perhaps expanding gas directly enters a subcooler, make product gas again in main heat exchanger after the re-heat, wherein a part of nitrogen enters and makes heated air in the molecular sieve adsorber.
I. the crude argon column top is provided with a condenser, introduce pressure column condensed oxygen enrichment in bottom or pure oxygen liquid, after crossing cold decompression, subcooler enters the low-temperature receiver of making tower in the crude argon column condenser, by the set column plate section argon enrichment region in bottom, lower pressure column oxygen enriched liquid porch, drawing a part of argon fraction gas enters the crude argon column bottom and makes unstripped gas, in tower after the rectifying, discharge small amount of exhaust gas in the crude argon overhead condenser, the liquid of crude argon column bottom still returns into the lower pressure column corresponding site, crude argon then draws at the crude argon column top, and the oxygen rich air of being evaporated in the condenser is still returned in the lower pressure column.
10, pressure column is set up the air separation equipment flow process of a crude argon column, its feature:
A. the crude argon column top is provided with a condenser, and the condensation liquid oxygen of introducing rectifier bottoms enters the low-temperature receiver that condenser is made tower after lowering the temperature through cold decompression.
B. pressure column purifies the set column plate section middle part argon fraction enrichment region in bottom, raw air porch and draws a part of argon fraction gas and enter the crude argon column bottom and make unstripped gas.
C. after the rectifying, the phegma that is obtained at the bottom of tower still returns into the pressure column corresponding site unstripped gas in crude argon column.
D. liquid oxygen is evaporated in the condenser that enters the crude argon column top, and evaporation oxygen still returns out in the low oxygen pipeline that rectifying column top condenser evaporated.
E. unstripped gas after the rectifying, is discharged small amount of exhaust gas in overhead condenser in crude argon column, and crude argon is then drawn at the crude argon column top.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 96116391 CN1168464A (en) | 1996-06-17 | 1996-06-17 | Air separating method and equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 96116391 CN1168464A (en) | 1996-06-17 | 1996-06-17 | Air separating method and equipment |
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| CN1168464A true CN1168464A (en) | 1997-12-24 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 96116391 Pending CN1168464A (en) | 1996-06-17 | 1996-06-17 | Air separating method and equipment |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103292576A (en) * | 2012-02-29 | 2013-09-11 | 乔治洛德方法研究和开发液化空气有限公司 | Process and apparatus for the separation of air by cryogenic distillation |
| CN104776685A (en) * | 2014-03-19 | 2015-07-15 | 摩尔动力(北京)技术股份有限公司 | Method and system for preparing low-oxygen liquid nitrogen |
| CN105865148A (en) * | 2016-04-01 | 2016-08-17 | 上海启元空分技术发展股份有限公司 | Method for efficient production of high-purity oxygen and high-purity nitrogen |
| CN106016968A (en) * | 2016-07-14 | 2016-10-12 | 王嘉文 | Method and device for liquidation purification of carbon dioxide |
| CN107606874A (en) * | 2017-10-26 | 2018-01-19 | 上海联风能源科技有限公司 | A kind of device of Full distillation purification recovery argon gas and its method for reclaiming argon gas |
| CN113606867A (en) * | 2021-08-14 | 2021-11-05 | 张家港市东南气体灌装有限公司 | Air separation device and method capable of realizing interchange of internal and external oxygen compression processes |
| CN113790575A (en) * | 2021-09-17 | 2021-12-14 | 东台宏仁气体有限公司 | High-purity oxygen manufacturing device and preparation method thereof |
-
1996
- 1996-06-17 CN CN 96116391 patent/CN1168464A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103292576A (en) * | 2012-02-29 | 2013-09-11 | 乔治洛德方法研究和开发液化空气有限公司 | Process and apparatus for the separation of air by cryogenic distillation |
| CN104776685A (en) * | 2014-03-19 | 2015-07-15 | 摩尔动力(北京)技术股份有限公司 | Method and system for preparing low-oxygen liquid nitrogen |
| CN105865148A (en) * | 2016-04-01 | 2016-08-17 | 上海启元空分技术发展股份有限公司 | Method for efficient production of high-purity oxygen and high-purity nitrogen |
| CN106016968A (en) * | 2016-07-14 | 2016-10-12 | 王嘉文 | Method and device for liquidation purification of carbon dioxide |
| CN107606874A (en) * | 2017-10-26 | 2018-01-19 | 上海联风能源科技有限公司 | A kind of device of Full distillation purification recovery argon gas and its method for reclaiming argon gas |
| CN107606874B (en) * | 2017-10-26 | 2023-06-23 | 上海联风能源科技有限公司 | Device for recycling argon through full rectification purification and argon recycling method thereof |
| CN113606867A (en) * | 2021-08-14 | 2021-11-05 | 张家港市东南气体灌装有限公司 | Air separation device and method capable of realizing interchange of internal and external oxygen compression processes |
| CN113606867B (en) * | 2021-08-14 | 2022-12-02 | 张家港市东南气体灌装有限公司 | Air separation device and method capable of realizing interchange of internal and external oxygen compression processes |
| CN113790575A (en) * | 2021-09-17 | 2021-12-14 | 东台宏仁气体有限公司 | High-purity oxygen manufacturing device and preparation method thereof |
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