CN1076269A - Air separating method and equipment - Google Patents
Air separating method and equipment Download PDFInfo
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- CN1076269A CN1076269A CN 92108349 CN92108349A CN1076269A CN 1076269 A CN1076269 A CN 1076269A CN 92108349 CN92108349 CN 92108349 CN 92108349 A CN92108349 A CN 92108349A CN 1076269 A CN1076269 A CN 1076269A
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- C01B21/00—Nitrogen; Compounds thereof
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/508—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by selective and reversible uptake by an appropriate medium, i.e. the uptake being based on physical or chemical sorption phenomena or on reversible chemical reactions
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Abstract
The present invention relates to a kind of air separating method and equipment, promptly is to come separation of air by the principle of cryogenic rectification, produces the method and apparatus of oxygen, nitrogen, argon.It can be a kind of ultralow pressure flow process, under extremely low energy consumption condition, produce 99.99～99.9999% high purity nitrogen products by a single rectification column, can also produce simultaneously that to contain oxygen be 60～98% oxygen rich gas, proposition reaches the method and apparatus of producing crude argon on single rectification column in the method that adopts pressuring expansion on the single rectification column, and oxygen, nitrogen, argon are all had extra high recovery rate.
Description
The present invention relates to a kind of air separating method and equipment, promptly is to come separation of air by the principle of cryogenic rectification, produces the method and apparatus of oxygen, nitrogen, argon.
Air separation adopts rectifying column to finish, and German patent DE 3610973A1 discloses a kind of single rectification column flow process with the supercharger expansion, produces 99.9999% high pure nitrogen.This air separating method is that raw air is compressed to enter behind the 6bar pressure in compressor and removes moisture content, carbon dioxide, acetylene and hydrocarbon partial in the molecular sieve adsorber, be divided into two the tunnel then, wherein 40% purification raw air enters and is cooled to the liquia air that enters heating tower's still in the set boiler channel of rectifier bottoms after about 100K temperature in the main heat exchanger, goes out behind the evaporimeter to cut down by a throttling to enter the rectifying column middle part after being decompressed to 4bar pressure.After another road accounts for 60% raw air be pressurized to 7bar pressure in the supercharger of decompressor, entering in the main heat exchanger gas cooled of being backflowed again enters after the 120K temperature and makes adiabatic expansion in the decompressor, enter in the rectifying column after being expanded to 4bar pressure, rectifier bottoms obtains to contain the higher liquia air of oxygen, after drawing tower, again through the cold excessively low-temperature receiver of making tower in the set condenser/evaporator in rectifying column top that enters of subcooler, can obtain 99.9999% high pure nitrogen at the rectifying column top.The advantage of this invention is because raw air is pressurized, therefore enter the corresponding minimizing of expanded air amount in the tower, and improved the rectification effect of tower, on the other hand, because liquia air is heated by one hot air, therefore, can obtain to contain the higher liquia air of oxygen, make nitrogen output that raising arranged.
The deficiency of this invention is first: because the air themperature that feeds in the tower still evaporimeter is about 100K, can obtain to contain oxygen and be 36～50% liquia air at the bottom of tower, therefore, the recovery rate of high purity nitrogen output increases, but the leeway that also improves a lot.Second: rectifying column pressure is higher, and the pressure of compressor is corresponding higher, and therefore, energy consumption is higher.The 3rd: oxygen is too low can't to be utilized liquia air because of containing, and it is poor to fully utilize.
Task of the present invention is to propose a kind of air separating method and equipment, and it can be a kind of ultralow pressure flow process, and it produces 99.99～99.9999% high purity nitrogen products by a single rectification column under extremely low energy consumption condition; Can also produce simultaneously that to contain oxygen be 60～98% oxygen rich gas, proposing all has extra high recovery rate adopting the method for pressuring expansion on the single rectification column and produce the method and apparatus of crude argon on single rectification column to oxygen, nitrogen, argon.
Task of the present invention is to solve by following method, a kind of air separating method of cryogenic rectification, it is to remove moisture content in the molecular sieve adsorber entering after the compressed raw air cooling, carbon dioxide, acetylene and other hydrocarbon partials, form and purify raw air, one of method is to purify raw air to be divided into two parts, wherein a part enters main heat exchanger and is cooled near entering rectifying column middle part after the condensing temperature, the supercharger that another part then enters decompressor carries out supercharging, the air duct that raw air after the supercharging enters main heat exchanger is backflowed gas cooled to uniform temperature, entering the raw air of doing in the decompressor after adiabatic expansion or the supercharging more directly enters decompressor and makes adiabatic expansion, expanding gas then enters in the set evaporimeter of rectifier bottoms, liquia air at the bottom of the heating tower, and the temperature of control liquia air is under operating pressure, the oxygen content of liquia air was at 40～nearly 100% o'clock pairing temperature value, must control the liquia air temperature and be lower than and contain oxygen nearly 100% pairing temperature value under the operating pressure, the raw air that is cooled enters the rectifying column middle part after the cooling liquid after going out evaporimeter once more in heat exchanger; Two of method is that the purification raw air that molecular sieve all enters the rectifying column middle part, by a part by gas at normal temperature with pressure that air separation unit separated, enter again in the supercharger of decompressor and carry out supercharging, directly or again enter to be cooled in the main heat exchanger to enter after the uniform temperature and make adiabatic expansion in the decompressor, gas after the expansion then enters in the evaporimeter of rectifier bottoms and makes heated air, the heating liquid air, and the oxygen content of control liquia air temperature liquia air under operating pressure was at 40～nearly 100% o'clock pairing temperature value, must control the liquia air temperature and be lower than and contain nearly 100% o'clock pairing temperature value of oxygen under the operating pressure, divided gas flow is cooled out behind the evaporimeter then in main heat exchanger re-heat to normal temperature.Between bottom, raw air porch and tower still evaporimeter, a column plate section is set.A condenser is set at the rectifying column top, uprising gas in the condensing tower, its low-temperature receiver is after drawing tower by a part of liquid nitrogen that is condensed in the rectifying column, after heat exchanger is crossed cold decompression, enter the low-temperature receiver that condenser low pressure is made tower again, can obtain the temperature difference more than the 1.3K by the pressure of the minimum about 0.02～0.15MPa of pressure differential in condenser two sides.
The separated gas of an introducing part enters makes regeneration gas in the molecular sieve adsorber.
For the sky branch flow process of carrying argon, there is an argon enrichment region at the column plate section middle part set in the bottom, purification raw air porch of rectifying column, extracting a part of argon fraction gas out at the argon enrichment region enters crude argon column bottom and makes unstripped gas, be provided with a condenser at the crude argon column top, with uprising gas in the condensation crude argon column, the condensed fluid of crude argon column bottom still returns into the rectifying column corresponding site from the liquid nitrogen at rectifying column top in feeding.Can obtain crude argon gas at the crude argon column top.
The air separation equipment of 1 one kinds of cryogenic rectifications, its rectifying column are a lower pressure column, and the air separation equipment flow process of a crude argon column pressuring expansion is characterized by:
The compressed raw air of a is removed moisture content, carbon dioxide, acetylene and other hydrocarbon partials at molecular sieve adsorber and is formed the purification raw air.
B purifies raw air and is divided into two parts, wherein a part enter be pressurized in the supercharger of decompressor laggard go into draw from the main heat exchanger middle part again after main heat exchanger is cooled, enter that decompressor is made adiabatic expansion or the raw air that is pressurized directly enters and makes adiabatic expansion in the decompressor, expanding gas enters the liquia air in the heated base tower still in pressure column bottom and the evaporimeter again, and another part then enters to the saturated vapor in the middle part of the pressure column through the main heat exchanger gas cooled of being backflowed.
C lower pressure column top is provided with a condenser, by the pure liquid nitrogen of the part of lower pressure column top condensation through a subcooler cross cold after, after a pressure-reducing valve decompression cooling, enter the low-temperature receiver that condenser nitrogen side is made tower again, tower bottom is provided with an evaporimeter, enter and go out evaporimeter after the purification raw air of making thermal source in the evaporimeter is cooled off by liquia air, advancing a heat exchanger is again backflowed after the gas cooled liquefaction, enter the lower pressure column middle part and make phegma, between purification raw air porch and bottom evaporimeter, a column plate section is set.
The oxygen rich gas that d draws from lower pressure column bottom mixes afterwards main heat exchanger after the re-heat ejector and makes oxygen enriched product with the part oxygen enriched liquid that tower still bottom is drawn.
E crude argon column top is provided with a condenser, the condensation liquid nitrogen of drawing the lower pressure column top is made the low-temperature receiver of crude argon column, and draw a part of argon fraction gas by the set column plate section in the bottom, purification raw air porch of lower pressure column saturated vapor middle part argon enrichment region, enter the crude argon column bottom and make unstripped gas, rectifying crude argon column evaporator overhead condenser is discharged small amount of exhaust gas in crude argon column, the liquid that is condensed flows into the crude argon column bottom in lower pressure column, and crude argon is then drawn at the top of crude argon column.
Low-pressure nitrogen ejector after the heat exchanger package re-heat that f evaporates in the lower pressure column evaporator overhead condenser, a part is made the low-pressure nitrogen product, and another part is made the regeneration gas of molecular sieve adsorber.
After the pure gas nitrogen of pressure that pure gas nitrogen of pressure that g draws from the lower pressure column top and crude argon column condenser are evaporated converges, after the heat exchanger package re-heat, draw and obtain the high purity nitrogen product of pressure, in the condenser at lower pressure column top, can obtain the high-purity liquid nitrogen product.
The air separation equipment of 2 one kinds of cryogenic rectifications, its rectifying column are the air separation equipment flow process of the pressuring expansion of a lower pressure column, it is characterized by:
The compressed raw air of a is removed moisture content, carbon dioxide, acetylene and other hydrocarbonizes and thing formation purification raw air at molecular sieve adsorber.
B purifies raw air and is divided into two parts, wherein a part enter be pressurized in the supercharger of decompressor laggard go into draw from the main heat exchanger middle part again after main heat exchanger is cooled, enter that decompressor is made adiabatic expansion or the raw air that is pressurized directly enters decompressor and makes adiabatic expansion, expanding gas enters the liquia air in the heated base tower still in the evaporimeter of pressure column bottom again, and another part then enters the lower pressure column middle part through the main heat exchanger gas cooled of being backflowed to saturated vapor.
C lower pressure column top is provided with a condenser, by the pure liquid nitrogen of the part of lower pressure column top condensation through a subcooler cross cold after, after a pressure-reducing valve decompression cooling, enter the low-temperature receiver that condenser nitrogen side is made tower again, the lower pressure column bottom is provided with an evaporimeter, enter and go out evaporimeter after the purification raw air of making thermal source in the evaporimeter is cooled off by liquia air, advancing a heat exchanger is again backflowed after the gas cooled liquefaction, enter the pressure column middle part and make phegma, between purification raw air porch and bottom evaporimeter, a column plate section is set.
After the part oxygen enriched liquid that d is drawn bottom the tower still from the oxygen rich gas that the column plate of lower pressure column bottom is drawn mixed, ejector was made oxygen enriched product after the main heat exchanger re-heat.
Low-pressure nitrogen ejector after the heat exchanger package re-heat that e evaporates in the lower pressure column evaporator overhead condenser, a part is made the low-pressure nitrogen product, and another part is made the regeneration gas of molecular sieve adsorber.
The pure gas nitrogen of the pressure of f at lower pressure column top ejector after the heat exchanger package re-heat is made the high purity nitrogen product of pressure, can obtain pure liquid nitrogen product in the condenser at lower pressure column top.
The air separation equipment of 3 one kinds of cryogenic rectifications, its rectifying column are a pressure column, and the air separation equipment flow process of a crude argon column pressuring expansion is characterized by:
The compressed raw air of a removes moisture content, carbon dioxide, acetylene and other part hydrocarbonizes in molecular sieve adsorber and thing forms the purification raw air.
B purifies and to enter the pressure column middle part after raw air enters the gas cooled of being backflowed behind the main heat exchanger.
C pressure column top is provided with a condenser, by the pure liquid nitrogen of the part of pressure column top condensation through a subcooler cross cold after, after a pressure-reducing valve decompression cooling, enter the low-temperature receiver that condenser nitrogen side is made tower again, the pressure column bottom is provided with an evaporimeter, enter and go out evaporimeter after the expanding gas of making thermal source in the evaporimeter is cooled off by liquia air, enter the main heat exchanger re-heat again and to normal temperature, go out device, between purification raw air porch and bottom evaporimeter, a column plate section is set.
After the part oxygen enriched liquid that d is drawn bottom the tower still from the oxygen rich gas that draw the pressure column bottom mixed, ejector was made oxygen enriched product after the main heat exchanger re-heat.
E crude argon column top is provided with a condenser, the condensation liquid nitrogen of introducing the pressure column top is made the low-temperature receiver of crude argon column, and locate the set column plate section middle part argon enrichment region in bottom by the purification feed(raw material)inlet of pressure column saturated vapor and draw a part of argon fraction gas, enter the crude argon column bottom and make unstripped gas, in crude argon column after the rectifying, discharge small amount of exhaust gas at the crude argon column evaporator overhead condenser, the liquid that is condensed flows into the crude argon column bottom in pressure column, and crude argon is then drawn at the top of crude argon column.
Nitrogen ejector after the heat exchanger package re-heat that f evaporates in the pressure column evaporator overhead condenser, a part is made nitrogen product, and another part is made the regeneration gas of molecular sieve adsorber.
G draws after the pure gas nitrogen of pressure that the pure gas nitrogen of pressure and crude argon column condenser evaporated converges from the pressure column top, draws after the heat exchanger package re-heat and obtains the high purity nitrogen product of pressure, can obtain the high-purity liquid nitrogen product in the condenser at pressure column top.
The expanding gas source that h enters decompressor is 1) pressure nitrogen gas of drawing from the pressure column top, 2) or the pure nitrogen gas that evaporated from the pressure column evaporator overhead condenser, 3) or the pressure oxygen rich air of drawing from the pressure column bottom.Enter after they are compressed in the main heat exchanger re-heat enters the supercharger of decompressor to the normal temperature and make adiabatic expansion in the decompressor, perhaps enter 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 evaporimeter of pressure column bottom and makes heated air.
The air separation equipment of 4 one kinds of cryogenic rectifications, its rectifying column are the air separation equipment flow process of a pressure column pressuring expansion, it is characterized by:
The compressed raw air of a removes moisture content, carbon dioxide, acetylene and other part hydrocarbonizes in molecular sieve adsorber and thing forms the purification raw air.
B purifies and to enter the pressure column middle part after raw air enters the gas cooled of being backflowed behind the main heat exchanger.
C pressure column top is provided with a condenser, by the pure liquid nitrogen of the part of pressure column top condensation through a subcooler cross cold after, after a pressure-reducing valve decompression cooling, enter the low-temperature receiver that condenser nitrogen side is made tower again, the pressure column bottom is provided with an evaporimeter, enter and go out evaporimeter after the expanding gas of making thermal source in the evaporimeter is cooled off by liquia air, enter the main heat exchanger re-heat again and to normal temperature, go out device, between purification raw air porch and bottom evaporimeter, be provided with a column plate section.
After the part oxygen enriched liquid that d is drawn bottom the tower still from the oxygen rich gas that draw the pressure column bottom mixed, ejector was made oxygen enriched product after the re-heat in main heat exchanger.
Low-pressure nitrogen ejector after the heat exchanger package re-heat that e evaporates in the pressure column evaporator overhead condenser, a part is made the low-pressure nitrogen product, and another part is made the regeneration gas of molecular sieve adsorber.
The pure gas nitrogen of the pressure of f at pressure column top ejector after the heat exchanger package re-heat is made the high purity nitrogen product of pressure, can obtain pure liquid nitrogen product in the condenser at pressure column top.
The expanding gas source that g enters decompressor is 1) pressure nitrogen gas of drawing from the pressure column top, 2) or the pure nitrogen gas that evaporated from the pressure column evaporator overhead condenser, 3) or the pressure oxygen rich air of drawing from the pressure column bottom.Enter decompressor after they are compressed and make adiabatic expansion in the main heat exchanger re-heat enters the supercharger of decompressor to the normal temperature respectively, perhaps enter 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 evaporimeter of pressure column bottom and makes heated air.
Below in conjunction with flow chart, various air separation equipment flow processs are described.
Fig. 1 rectifying column is a lower pressure column, the air separation equipment flow process of a crude argon column pressuring expansion;
Fig. 2 rectifying column is the air separation equipment flow process of a lower pressure column pressuring expansion;
Fig. 3 rectifying column is a pressure column, crude argon column air device flow process that gas boosting expands of backflowing;
Fig. 4 rectifying column is the pressure column air device flow process that gas boosting expands of backflowing;
Fig. 1 is that rectifying column is a lower pressure column, the air separation equipment flow process of a crude argon column pressuring expansion.Raw air enters compressor 2 by pipeline 1 and is compressed to 0.25～1MPa pressure, the cooling back enters molecular sieve adsorber 4 by pipeline 3 and removes moisture content, carbon dioxide, acetylene and other hydrocarbons, through pipeline 5, main heat exchanger 6 gas cooled of being backflowed reaches capacity after the vapor (steam) temperature, through pipeline 7 decompression cut down 8 be decompressed to be not less than 150kPa pressure after, enter the rectifying column middle part through pipeline 9, drawing on the pipeline 5 after a part of raw air is pressurized in pipeline 20 enters the supercharger 21 of decompressor, draw in the air duct that enters in the main heat exchanger 6 by pipeline 22, after being cooled to uniform temperature, draw by pipeline 23, enter and make adiabatic expansion or this part raw air in the decompressor 24 after supercharger 21 is pressurized, enter decompressor 24 by pipeline 22a and make adiabatic expansion, expanding gas enters the liquia air in heating tower's still in the set evaporimeter 26 in tower 10 bottoms by pipeline 25, control liquia air temperature is lower than that liquia air contains nearly 100% o'clock pairing temperature value of oxygen under the operating pressure, the expanded air that is cooled goes out evaporimeter 26 back and enters heat exchanger 28 by pipeline 27 and backflowed gas cooled to saturated vapor, enters rectifying column 10 middle parts through pipeline 29 and carries out rectifying.On the column plate on tower still top, draw the oxygen rich gas that contains oxygen about 60～98%, enter main heat exchanger 6 through pipeline 14.In order to prevent in the tower still gathering of hydrocarbon such as acetylene in the oxygen enriched liquid and blast, enter in the oxygen rich gas drawing a part of liquia air by pipeline 16 at the bottom of the tower, together through main heat exchanger 6 re-heats to normal temperature, draw by pipeline 15 and to make product gas.One section column plate section 10a is set between set evaporimeter 26 in rectifying column 10 bottoms and the raw air inlet tube 9.Uprising gas is by 11 condensations of overhead condenser in the rectifying column 10, the pure liquid nitrogen part of condensation is made the phegma of tower, another part then drawn through pipeline 30 liquid nitrogen subcoolers 31 backflowed gas nitrogen cross cold after, through pipeline 32, decompression is cut down 33 decompression cooling backs and is entered the low-temperature receiver that condenser 11 low-pressure sides are made tower by pipeline 34, the low-pressure nitrogen that condenser 11 is evaporated by pipeline 40 through the heat exchanger package re-heat to normal temperature, draw by pipeline 42 and to make low pressure nitrogen product gas, wherein a part enters molecular sieve adsorber 4 through pipeline 43 and makes regeneration gas, again by pipeline 44 emptying.After high pure nitrogen was then drawn tower by pipeline 35, through heat exchanger 28, pipeline 36 was drawn by pipeline 37 to the normal temperature in main heat exchanger 6 re-heats and is made the high pure nitrogen product.
The stream of crude argon column is that crude argon column 50 tops are provided with a condenser 51, the argon enrichment region is drawn one argon fraction gas from the set column plate section 10a in raw air inlet duct 9 belows of rectifying column 10, enter crude argon column 50 bottoms through pipeline 54, oxygen in the uprising gas by crude argon condenser 51 condensations after its phegma still go into for 55 times in the pressure column 10 by pipeline, wherein part from rectifying column 10 pure liquid nitrogen that draw at the top, in entering crude argon column condenser 51, pipeline 52 makes the low-temperature receiver of tower, discharge small amount of exhaust gas by pipeline 57 in crude argon column 50 evaporator overhead condensers 51, crude argon is then drawn by pipeline 56 from crude argon column 51 tops, further remove micro amount of oxygen in the crude argon according to conventional method again, nitrogen, promptly obtain straight argon, this exceeds the scope that relates to of the present invention.
Fig. 2 is that rectifying column is a lower pressure column, the air separation equipment flow process of pressuring expansion.
Compared to Figure 1 its change part is to cancel the crude argon column 50 and the corresponding pipeline of crude argon system, and the oxygen rich air introduction pipe can be changed among the column plate section 10a that sets up and draw on the column plate below the argon enrichment region, is beneficial to reduce the argon in the purity nitrogen.
Fig. 3 is that rectifying column is a pressure column, crude argon column air separation equipment flow process that gas boosting expands of backflowing.
Compared to Figure 1 its change part is:
1) all enters tower 10 middle parts after being compressed the raw air cooling of purification.
2) enter the pressure nitrogen gas (comprising the pressure nitrogen gas that crude argon condenser 51 is evaporated) that the expanding gas of the supercharger of decompressor can be drawn by pressure nitrogen gas that is evaporated in the condenser 11 or pressure column 10 tops, or the pressure oxygen rich gas is drawn in pressure column 10 bottoms, all enter supercharger 21 to the normal temperature, then directly or enter decompressor 24 after the cooling and make adiabatic expansion in the heat exchanger package re-heat.
3) expanding gas enters evaporimeter 26, goes out evaporimeter after being cooled, and enters main heat exchanger 6 re-heats by pipeline 27 and make product gas to normal temperature.
Fig. 4 is that rectifying column is the pressure column air separation equipment flow process that gas boosting expands of backflowing.
Compare the crude argon column 50 and the corresponding pipeline of cancellation crude argon system in its change part with Fig. 3, the oxygen rich air introduction pipe can be changed among the column plate section 10a that sets up and draw on the column plate below the argon enrichment region, is beneficial to reduce the argon in the purity nitrogen.
Claims (7)
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 near saturated-steam temperature by heat exchanger, enter rectifying column then and carry out the rectifying separation, it is characterized in that purifying the pressure column middle part that raw air is introduced rectifying column, in the pressure column bottom, be provided with evaporimeter, be used for the liquia air at the bottom of the heating tower, control liquia air temperature under operating pressure liquia air content 40～temperature value of nearly 100% o'clock correspondence, uprising gas in the pressure column top is provided with the condenser condenses tower is provided with one section column plate section between pressure column introducing raw air porch and evaporimeter.Being arranged on the interior part heated air that feeds of evaporimeter of the bottom of rectifying column, is with pressure or the back low-pressure gas that expands, and this part gas is the purification raw air, or is separated gas.
2, 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 rectifying column purification bottom, raw air porch is set is drawn a part of argon fraction gas, feed the crude argon column bottom and make unstripped gas, the condensation liquid nitrogen 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 the rectifying column.
3, a kind of air separation equipment of cryogenic rectification, its rectifying column are a lower pressure column, and the air separation equipment flow process of a crude argon column pressuring expansion is characterized by:
The compressed raw air of a is removed moisture content, carbon dioxide, acetylene and other hydrocarbon partials at molecular sieve adsorber and is formed the purification raw air.
B purifies raw air and is divided into two parts, wherein a part enter be pressurized in the supercharger of decompressor laggard go into draw from the main heat exchanger middle part again after main heat exchanger is cooled, enter that decompressor is made adiabatic expansion or the raw air that is pressurized directly enters and makes adiabatic expansion in the decompressor, expanding gas enters the liquia air in the heated base tower still in pressure column bottom and the evaporimeter again, and another part then enters to the saturated vapor in the middle part of the pressure column through the main heat exchanger gas cooled of being backflowed.
C lower pressure column top is provided with a condenser, by the pure liquid nitrogen of the part of lower pressure column top condensation through a subcooler cross cold after, after a pressure-reducing valve decompression cooling, enter the low-temperature receiver that condenser nitrogen side is made tower again, tower bottom is provided with an evaporimeter, enter and go out evaporimeter after the purification raw air of making thermal source in the evaporimeter is cooled off by liquia air, advancing a heat exchanger is again backflowed after the gas cooled liquefaction, enter the lower pressure column middle part and make phegma, between purification raw air porch and bottom evaporimeter, a column plate section is set.
The oxygen rich gas that d draws from lower pressure column bottom mixes afterwards main heat exchanger after the re-heat ejector and makes oxygen enriched product with the part oxygen enriched liquid that tower still bottom is drawn.
E crude argon column top is provided with a condenser, the condensation liquid nitrogen of drawing the lower pressure column top is made the low-temperature receiver of crude argon column, and draw a part of argon fraction gas by the set column plate section in the bottom, purification raw air porch of lower pressure column saturated vapor middle part argon enrichment region, enter the crude argon column bottom and make unstripped gas rectifying crude argon column evaporator overhead condenser discharge small amount of exhaust gas in crude argon column, the liquid that is condensed flows into the crude argon column bottom in lower pressure column, and crude argon is then drawn at the top of crude argon column.
Low-pressure nitrogen ejector after the heat exchanger package re-heat that f evaporates in the lower pressure column evaporator overhead condenser, a part is made the low-pressure nitrogen product, and another part is made the regeneration gas of molecular sieve adsorber.
After the pure gas nitrogen of pressure that pure gas nitrogen of pressure that g draws from the lower pressure column top and crude argon column condenser are evaporated converges, after the heat exchanger package re-heat, draw and obtain the high purity nitrogen product of pressure, in the condenser at lower pressure column top, can obtain the high-purity liquid nitrogen product.
4, a kind of air separation equipment of cryogenic rectification, its rectifying column are the air separation equipment flow process of the pressuring expansion of a lower pressure column, it is characterized by:
The compressed raw air of a is removed moisture content, carbon dioxide, acetylene and other hydrocarbonizes and thing formation purification raw air at molecular sieve adsorber.
B purifies raw air and is divided into two parts, wherein a part enter be pressurized in the supercharger of decompressor laggard go into draw from the main heat exchanger middle part again after main heat exchanger is cooled, enter that decompressor is made adiabatic expansion or the raw air that is pressurized directly enters decompressor and makes adiabatic expansion, expanding gas enters the liquia air in the heated base tower still in the evaporimeter of pressure column bottom again, and another part then enters the lower pressure column middle part through the main heat exchanger gas cooled of being backflowed to saturated vapor.
C lower pressure column top is provided with a condenser, by the pure liquid nitrogen of the part of lower pressure column top condensation through a subcooler cross cold after, after a pressure-reducing valve decompression cooling, enter the low-temperature receiver that condenser nitrogen side is made tower again, the lower pressure column bottom is provided with an evaporimeter, enter and go out evaporimeter after the purification raw air of making thermal source in the evaporimeter is cooled off by liquia air, advancing a heat exchanger is again backflowed after the gas cooled liquefaction, enter the pressure column middle part and make phegma, between purification raw air porch and bottom evaporimeter, a column plate section is set.
After the part oxygen enriched liquid that d is drawn bottom the tower still from the oxygen rich gas that the column plate of lower pressure column bottom is drawn mixed, ejector was made oxygen enriched product after the main heat exchanger re-heat.
Low-pressure nitrogen ejector after the heat exchanger package re-heat that e evaporates in the lower pressure column evaporator overhead condenser, a part is made the low-pressure nitrogen product, and another part is made the regeneration gas of molecular sieve adsorber.
The pure gas nitrogen of the pressure of f at lower pressure column top ejector after the heat exchanger package re-heat is made the high purity nitrogen product of pressure, can obtain pure liquid nitrogen product in the condenser at lower pressure column top.
5, a kind of air separation equipment of cryogenic rectification, its rectifying column are a pressure column, and the air separation equipment flow process of a crude argon column pressuring expansion is characterized by:
The compressed raw air of a removes moisture content, carbon dioxide, acetylene and other part hydrocarbonizes in molecular sieve adsorber and thing forms the purification raw air.
B purifies and to enter the pressure column middle part after raw air enters the gas cooled of being backflowed behind the main heat exchanger.
C pressure column top is provided with a condenser, by the pure liquid nitrogen of the part of pressure column top condensation through a subcooler cross cold after, after a pressure-reducing valve decompression cooling, enter the low-temperature receiver that condenser nitrogen side is made tower again, the pressure column bottom is provided with an evaporimeter, enter and go out evaporimeter after the expanding gas of making thermal source in the evaporimeter is cooled off by liquia air, enter the main heat exchanger re-heat again and to normal temperature, go out device, between purification raw air porch and bottom evaporimeter, a column plate section is set.
After the part oxygen enriched liquid that d is drawn bottom the tower still from the oxygen rich gas that draw the pressure column bottom mixed, ejector was made oxygen enriched product after the main heat exchanger re-heat.
E crude argon column top is provided with a condenser, the condensation liquid nitrogen of introducing the pressure column top is made the low-temperature receiver of crude argon column, and locate the set column plate section middle part argon enrichment region in bottom by the purification feed(raw material)inlet of pressure column saturated vapor and draw a part of argon fraction gas, enter the crude argon column bottom and make unstripped gas, in crude argon column after the rectifying, discharge small amount of exhaust gas at the crude argon column evaporator overhead condenser, the liquid that is condensed flows into the crude argon column bottom in pressure column, and crude argon is then drawn at the top of crude argon column.
Nitrogen ejector after the heat exchanger package re-heat that f evaporates in the pressure column evaporator overhead condenser, a part is made nitrogen product, and another part is made the regeneration gas of molecular sieve adsorber.
G draws after the pure gas nitrogen of pressure that the pure gas nitrogen of pressure and crude argon column condenser evaporated converges from the pressure column top, draws after the heat exchanger package re-heat and obtains the high purity nitrogen product of pressure, can obtain the high-purity liquid nitrogen product in the condenser at pressure column top.
The expanding gas source that h enters decompressor is 1) pressure nitrogen gas of drawing from the pressure column top, 2) or the pure nitrogen gas that evaporated from the pressure column evaporator overhead condenser, 3) or the pressure oxygen rich air of drawing from the pressure column bottom.Enter after they are compressed in the main heat exchanger re-heat enters the supercharger of decompressor to the normal temperature and make adiabatic expansion in the decompressor, perhaps enter 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 evaporimeter of pressure column bottom and makes heated air.
6, a kind of air separation equipment of cryogenic rectification, its rectifying column are the air separation equipment flow process of a pressure column pressuring expansion, it is characterized by:
The compressed raw air of a removes moisture content, carbon dioxide, acetylene and other part hydrocarbonizes in molecular sieve adsorber and thing forms the purification raw air.
B purifies and to enter the pressure column middle part after raw air enters the gas cooled of being backflowed behind the main heat exchanger.
C pressure column top is provided with a condenser, by the pure liquid nitrogen of the part of pressure column top condensation through a subcooler cross cold after, after a pressure-reducing valve decompression cooling, enter the low-temperature receiver that condenser nitrogen side is made tower again, the pressure column bottom is provided with an evaporimeter, enter and go out evaporimeter after the expanding gas of making thermal source in the evaporimeter is cooled off by liquia air, enter the main heat exchanger re-heat again and to normal temperature, go out device, between purification raw air porch and bottom evaporimeter, be provided with a column plate section.
The oxygen rich gas that d draws from pressure column bottom mixes afterwards main heat exchanger after the re-heat ejector and makes oxygen enriched product with the part oxygen enriched liquid that tower still bottom is drawn.
Low-pressure nitrogen ejector after the heat exchanger package re-heat that e evaporates in the pressure column evaporator overhead condenser, a part is made the low-pressure nitrogen product, and another part is made the regeneration gas of molecular sieve adsorber.
The pure gas nitrogen of the pressure of f at pressure column top ejector after the heat exchanger package re-heat is made the high purity nitrogen product of pressure, can obtain pure liquid nitrogen product in the condenser at pressure column top.
The expanding gas source that g enters decompressor is 1) pressure nitrogen gas of drawing from the pressure column top, 2) or the pure nitrogen gas that evaporated from the pressure column evaporator overhead condenser, 3) or the pressure oxygen rich air of drawing from the pressure column bottom.Enter decompressor after they are compressed and make adiabatic expansion in the main heat exchanger re-heat enters the supercharger of decompressor to the normal temperature respectively, perhaps enter to be cooled in the main heat exchanger and enter decompressor after the uniform temperature again and make adiabatic expansion.Expanding gas then enters the interior heating source of the gas of doing of evaporimeter of pressure column bottom.
7, according to claim 5,6 described air separating methods, it is characterized in that on the oxygen rich gas passage after the main heat exchanger re-heat, perhaps the extension pressed gas enters supercharging the supercharger on the pressure nitrogen gas passage after re-heat, and in decompressor, make adiabatic expansion, expanding gas then enters in the tower still evaporimeter and makes heated air, goes out evaporimeter after go out device after the main heat exchanger re-heat and makes product gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 92108349 CN1076269A (en) | 1992-03-12 | 1992-03-12 | Air separating method and equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 92108349 CN1076269A (en) | 1992-03-12 | 1992-03-12 | Air separating method and equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1076269A true CN1076269A (en) | 1993-09-15 |
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ID=4943460
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 92108349 Pending CN1076269A (en) | 1992-03-12 | 1992-03-12 | Air separating method and equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1076269A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102322727A (en) * | 2011-09-08 | 2012-01-18 | 罗良宜 | Air energy air liquefaction separation device |
| CN102380361A (en) * | 2011-08-31 | 2012-03-21 | 莱芜钢铁股份有限公司 | Process utilizing product nitrogen gas to involve regeneration of molecular sieve absorbers |
| CN102494515A (en) * | 2011-12-05 | 2012-06-13 | 无锡威克亨盛机械制造有限公司 | Process for preparing high-pressure medical oxygen |
| CN102706101A (en) * | 2012-05-23 | 2012-10-03 | 苏州制氧机有限责任公司 | Air separating device |
| CN105423700A (en) * | 2014-09-09 | 2016-03-23 | 孙克锟 | Single-stage rectification equipment for separating air |
| CN105466155A (en) * | 2015-12-21 | 2016-04-06 | 七台河宝泰隆煤化工股份有限公司 | Air separation system |
-
1992
- 1992-03-12 CN CN 92108349 patent/CN1076269A/en active Pending
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102380361A (en) * | 2011-08-31 | 2012-03-21 | 莱芜钢铁股份有限公司 | Process utilizing product nitrogen gas to involve regeneration of molecular sieve absorbers |
| CN102380361B (en) * | 2011-08-31 | 2013-03-13 | 山东钢铁股份有限公司 | Process utilizing product nitrogen gas to involve regeneration of molecular sieve absorbers |
| CN102322727A (en) * | 2011-09-08 | 2012-01-18 | 罗良宜 | Air energy air liquefaction separation device |
| CN102494515A (en) * | 2011-12-05 | 2012-06-13 | 无锡威克亨盛机械制造有限公司 | Process for preparing high-pressure medical oxygen |
| CN102706101A (en) * | 2012-05-23 | 2012-10-03 | 苏州制氧机有限责任公司 | Air separating device |
| CN102706101B (en) * | 2012-05-23 | 2013-11-06 | 苏州制氧机有限责任公司 | Air separating device |
| CN105423700A (en) * | 2014-09-09 | 2016-03-23 | 孙克锟 | Single-stage rectification equipment for separating air |
| CN105423700B (en) * | 2014-09-09 | 2020-02-14 | 孙克锟 | Single-stage rectification equipment for separating air |
| CN105466155A (en) * | 2015-12-21 | 2016-04-06 | 七台河宝泰隆煤化工股份有限公司 | Air separation system |
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