US2918802A - Process of separation of air into its elements - Google Patents
Process of separation of air into its elements Download PDFInfo
- Publication number
- US2918802A US2918802A US612441A US61244156A US2918802A US 2918802 A US2918802 A US 2918802A US 612441 A US612441 A US 612441A US 61244156 A US61244156 A US 61244156A US 2918802 A US2918802 A US 2918802A
- Authority
- US
- United States
- Prior art keywords
- pressure
- air
- liquid
- expansion
- oxygen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 239000003570 air Substances 0.000 title claims description 33
- 238000000034 methods Methods 0.000 title claims description 14
- 238000000926 separation method Methods 0.000 title description 4
- 239000001301 oxygen Substances 0.000 claims description 23
- 229910052760 oxygen Inorganic materials 0.000 claims description 23
- 239000007788 liquids Substances 0.000 claims description 19
- 239000001308 nitrogen Substances 0.000 claims description 18
- 229910052757 nitrogen Inorganic materials 0.000 claims description 18
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 18
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,PD94bWwgdmVyc2lvbj0nMS4wJyBlbmNvZGluZz0naXNvLTg4NTktMSc/Pgo8c3ZnIHZlcnNpb249JzEuMScgYmFzZVByb2ZpbGU9J2Z1bGwnCiAgICAgICAgICAgICAgeG1sbnM9J2h0dHA6Ly93d3cudzMub3JnLzIwMDAvc3ZnJwogICAgICAgICAgICAgICAgICAgICAgeG1sbnM6cmRraXQ9J2h0dHA6Ly93d3cucmRraXQub3JnL3htbCcKICAgICAgICAgICAgICAgICAgICAgIHhtbG5zOnhsaW5rPSdodHRwOi8vd3d3LnczLm9yZy8xOTk5L3hsaW5rJwogICAgICAgICAgICAgICAgICB4bWw6c3BhY2U9J3ByZXNlcnZlJwp3aWR0aD0nODVweCcgaGVpZ2h0PSc4NXB4JyB2aWV3Qm94PScwIDAgODUgODUnPgo8IS0tIEVORCBPRiBIRUFERVIgLS0+CjxyZWN0IHN0eWxlPSdvcGFjaXR5OjEuMDtmaWxsOiNGRkZGRkY7c3Ryb2tlOm5vbmUnIHdpZHRoPSc4NScgaGVpZ2h0PSc4NScgeD0nMCcgeT0nMCc+IDwvcmVjdD4KPHBhdGggY2xhc3M9J2JvbmQtMCcgZD0nTSA2My4zMTU0LDQyIEwgMjAuNjg0Niw0Micgc3R5bGU9J2ZpbGw6bm9uZTtmaWxsLXJ1bGU6ZXZlbm9kZDtzdHJva2U6IzQyODRGNDtzdHJva2Utd2lkdGg6MnB4O3N0cm9rZS1saW5lY2FwOmJ1dHQ7c3Ryb2tlLWxpbmVqb2luOm1pdGVyO3N0cm9rZS1vcGFjaXR5OjEnIC8+CjxwYXRoIGNsYXNzPSdib25kLTAnIGQ9J00gNjMuMzE1NCwzMC4wMDk3IEwgMjAuNjg0NiwzMC4wMDk3JyBzdHlsZT0nZmlsbDpub25lO2ZpbGwtcnVsZTpldmVub2RkO3N0cm9rZTojNDI4NEY0O3N0cm9rZS13aWR0aDoycHg7c3Ryb2tlLWxpbmVjYXA6YnV0dDtzdHJva2UtbGluZWpvaW46bWl0ZXI7c3Ryb2tlLW9wYWNpdHk6MScgLz4KPHBhdGggY2xhc3M9J2JvbmQtMCcgZD0nTSA2My4zMTU0LDUzLjk5MDMgTCAyMC42ODQ2LDUzLjk5MDMnIHN0eWxlPSdmaWxsOm5vbmU7ZmlsbC1ydWxlOmV2ZW5vZGQ7c3Ryb2tlOiM0Mjg0RjQ7c3Ryb2tlLXdpZHRoOjJweDtzdHJva2UtbGluZWNhcDpidXR0O3N0cm9rZS1saW5lam9pbjptaXRlcjtzdHJva2Utb3BhY2l0eToxJyAvPgo8dGV4dCBkb21pbmFudC1iYXNlbGluZT0iY2VudHJhbCIgdGV4dC1hbmNob3I9InN0YXJ0IiB4PSc2NS4zMTM4JyB5PSc0NC45OTc2JyBzdHlsZT0nZm9udC1zaXplOjE5cHg7Zm9udC1zdHlsZTpub3JtYWw7Zm9udC13ZWlnaHQ6bm9ybWFsO2ZpbGwtb3BhY2l0eToxO3N0cm9rZTpub25lO2ZvbnQtZmFtaWx5OnNhbnMtc2VyaWY7ZmlsbDojNDI4NEY0JyA+PHRzcGFuPk48L3RzcGFuPjwvdGV4dD4KPHRleHQgZG9taW5hbnQtYmFzZWxpbmU9ImNlbnRyYWwiIHRleHQtYW5jaG9yPSJlbmQiIHg9JzE4LjY4NjInIHk9JzQ0Ljk5NzYnIHN0eWxlPSdmb250LXNpemU6MTlweDtmb250LXN0eWxlOm5vcm1hbDtmb250LXdlaWdodDpub3JtYWw7ZmlsbC1vcGFjaXR5OjE7c3Ryb2tlOm5vbmU7Zm9udC1mYW1pbHk6c2Fucy1zZXJpZjtmaWxsOiM0Mjg0RjQnID48dHNwYW4+TjwvdHNwYW4+PC90ZXh0Pgo8L3N2Zz4K N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 15
- 239000000727 fractions Substances 0.000 claims description 14
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 239000007789 gases Substances 0.000 description 13
- 238000009834 vaporization Methods 0.000 description 6
- 238000005057 refrigeration Methods 0.000 description 4
- 238000001816 cooling Methods 0.000 description 3
- 238000003303 reheating Methods 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- 281000178925 Liquid Air companies 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N carbon dioxide Chemical compound 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O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxides Inorganic materials 0.000 description 2
- 206010040003 Sensation of pressure Diseases 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
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- 238000005201 scrubbing Methods 0.000 description 1
- 239000000953 sodium hydroxide Substances 0.000 description 1
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- 229910001856 sodium hydroxide Inorganic materials 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
Images
Classifications
-
- 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
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
-
- 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
- F25J3/04315—Lowest pressure or impure nitrogen, so-called waste nitrogen expansion
-
- 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
-
- 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
- F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
-
- 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
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
Description
1386- 1959 J; F. GRUNBERG PROCESS OF SEPARATION OF AIR INTO ITS ELEMENTS Filed. Sept. 27, 1956 17zue/2ZZ/ JYCQUES FT GRUIVBFRG United States P n PROCESS OF SEPARATION OF AIR' INTO ITS ELEMENTS Jacques F. Grunberg, Outremont, Quebec, Canada, as-
signor to LAir Liquide, Societe Anonyme pour lEtude et l'Exploitation des Procedes Georges Claude, Paris, France, a body politic and corporate Application September 27, 1956, Serial No. 612,441
7 Claims. (CI. 62-25) section of the unit, or a part of the gaseous nitrogen.
obtained in the rectification high pressure column of a two-column rectification process.
It is characteristic of the present invention that the: low pressure stage used for the rectification is appre ciably higher than atmospheric pressure and that at least: one of the product gases delivered by the low pressure column is expanded, at least in part, with production of:'
external work.
As the flow of expanded gas can be important (for ex-- ample, the total amount of nitrogen product can be ex+' panded), the refrigeration produced is considerable, even for a relatively small expansion ratio, and it is possible: to produce all the refrigeration necessary for the operation of the unit in expanding nitrogen from a relatively lowpressure, for example, from 2 kg./cm. absolute pressure down to a pressure close to the atmospheric pres-- sure.
The expansion of the product gas can be carried out: in a turbine, this type of machine having a'high efficiency for low expansion ratios, and being particularly con-' venient when the actual volume of gases to be expanded. is relatively considerable. In the case of small units,. where generally reciprocating engines are used for the: expansion of high pressure air, the reciprocating engine: can be replaced by a turbine expanding low pressure nitrogen, as per the invention. The turbine will give greater running security, will be less cumbersome, and. cheaper than the conventional reciprocating expansion. engine.
It should be also noticed that, due to the low intake and discharge pressures of the turbine, smaller gas leaks will be experienced than on turbines running at higher" pressures.
The gas, which leaves the top of the low pressure column at a very low temperature, must first be reheated before expansion in order to increase the efliciency of' the expansion and avoid a partial liquefaction. In a preferred arrangement of the invention, the gas which must be expanded, is first reheated before expansion by heat transfer with a liquid leaving the high pressure column. The liquid is further expanded and delivered to a low pressure column.
Besides, the gas which is expanded in the turbine leavesit too cold to be sent directly to the heat exchanger sec-- tion destined to cool the air to be treated. In another type of arrangement of the present invenion, the expanded gas is reheated as above, by heat transfer with a liquid. leaving the high pressure column and sent to a low pressure column.
It is seen that for the reheating of the gas, before and" after expansion, the liquid coolers can be used. These liquid coolers are standard on these plants to reduce the: amount of liquid vaporized through the expansion. The" liquid coolers can be used as super heaters for the gas,. due to the relatively low temperature drop, which results from the expansion of the gas.
An interesting application of the present invention con-1- cerns the units where the separation of air produces'v gaseous oxygen under pressure through the vaporization.-
of liquid-oxygen compressed beforehand.
' It is well known that, in order to produce oxygenunder pressure, the compressed air to be separated is used both for the vaporization of the liquid-oxygen under pressure by heat transfer with the liquid-oxygen, and for the production of refrigeration through expansion with external work. Due to the fact that the vaporization of liquidperature of the oxygen, in order to obtain a good efiiciency oxygen under pressure requires a large amount of heat supplied at a relatively high temperature, it is necessary in the conventional processes to compress air at a pressure which is appreciably higher than that of the pro-' Y duced oxygen, so that the heat transfer can be carried out.
a If a part of the high pressure air has to be expanded with external work in the conventional processes, it is generally necessary to send it to the expansion engine at a temperature which is higher than the vaporization temof the expansion without partial liquefaction in the engine.
The total amount of air which remains available for the vaporization of the high pressure oxygen, is then reduced and the air pressure appreciably increased in order t compensate for the reduction of the output.
The present invention permits avoidance of the abovementioned inconveniences. Refrigeration is suppliedby expansion with external work of at least one of the product gases collected at one of the low pressures used for whereas the second fraction is sent after cooling at about its initial pressure to the rectification section of the plant.-
A non-limitative example has been described below and is illustrated in the attached drawing, which shows a unit made of two columns for the production of gaseous oxygen under pressure.
The atmospheric air to be separated is compressed in a blower 1 at an absolute pressure of about 8.5 kg./cm. and cooled in a water-cooler 2. It leaves the cooler at about 27 C. The air is then divided into two fractions. The first one (about 77.5% of the total of air treated) enters regenerator 4A through pipe 3 and loses its moisture and its carbon dioxide. The purified air leaves the regenerator at a temperature which is slightly higher than its dew point and, through pipe 6, enters the high pressure rectification column 18 at an absolute pressure of about 8.3 kg./cm. The second air fraction, about 22.5% of the total amount, is fed through pipe 7 to a compressor 8, where it is further compressed to a pressure high enough to allow the vaporization of the compressed liquid oxygen. If, for example, it is desired to produce oxygen under an absolute pressure of about 6.3 kg./cm. the air is compressed in the compressor 8 at an absolute pressure of about 21 kg./cm.
Through pipe 9, the air is fed to the water-cooler 10. It then enters the decarbonation tower 11, where carbon dioxide is removed through caustic soda scrubbing. The air is then dried in the desiccation unit 12 and sent through pipe 12A to the exchanger 13, then to the liquefier 14, in which the air is cooled down and liquefied by indirect heat exchange with the liquid-oxygen under pressure.
aaiaeoa Through pipe 15, the liquefied air enters coil 16, which is placed in the lower section of the high pressure column 18. In this coil, the high pressure liquid air is further cooled by indirect heat exchange with the liquid boiling in the lower part of this column. The liquid air is then expanded to an absolute pressure of 8.4 kg/cm. through valve 17, and sent to column 18. This column separates the air into two fractions: a liquid rich in oxygen, and liquid-nitrogen. The liquid rich in oxygen leaves the lower part of this column through pipe 19 and is then cooled down in exchanger 20. It is then filtered in ab sorption filter 21, in order to remove acetylene, and sent through valve 22 to the low pressure column 23. The high pressure column produces a second fraction which is liquid-nitrogen. This liquid-nitrogen leaves column 18 through pipe 24, is cooled in heat exchanger 25 and sent through valve 26 to the top of the low pressure column 23.
The low pressure column 23 works under an absolute pressure of about 2.1 kg./cm. It gives two products:
(a) Liquid-oxygen, which is later compressed to an absolute pressure of 6.3 kg./cm. through pump 27 and sent through pipe 27A to the exchangers 14 and 13, where it is heated, vaporized and finally reheated in the gaseous state, before leaving the unit approximately at ambient temperature.
(b) Gaseous nitrogen, which leaves the top of column 23, is reheated in heat exchanger 25, expanded to an absolute pressure of about 1.25 l g./c1n. in expansion turbine 28. It is then reheated in heat exchanger 20, before entering regenerator 48 through conduit 29. The nitrogen leaves the unit through pipe 30 at approximately ambient temperature and pressure.
I claim:
1. In a process of production of oxygen under pressure by the liquefaction and rectification of air in at least two rectifying zones under successively lower pressures, wherein the air to be separated is divided into two fractions, the first one of which is compressed to a higher pressure than the second one and cooled by heat exchange with liquid oxygen under pressure, then introduced into a rectifying zone and the second one of which is introduced under its original pressure into a rectifying zone, the improvement of maintaining a higher than atmospheric pressure in the rectifying zone under the lowest pressure, and expanding with external work the whole of the separated nitrogen from said lowest pressure to nearly atmospheric pressure.
2. A process according to claim 1, wherein the nitrogen is reheated before its expansion by heat exchange with a liquid leaving a rectification zone and sent to a lower pres! sure rectification zone.
3. A process according to claim 1, wherein the expanded nitrogen is reheated by heat exchange with a liquid originating from a rectification zone and sent to a lower pressure rectification zone.
4, A process of production of oxygen under pressure by the liquefaction and rectification of air in two rectification zones under successively lower pressures, comprising, compressing the air to be. separated, dividing it into two fractions, further compressing a first fraction of the air, cooling said fraction byheat exchange with liquid oxygen under pressure, introducing it into at least a rectification zone, cooling a second fraction of the air by heat exchange with cold gaseous nitrogen and introducing it under its original pressure into a rectification zone, compressing liquid oxygen issued from the lower pressure rectification zone and reheating it by heat exchange with said first fraction of the air, and expanding with external work the.
whole of the gaseous nitrogen issued from the lower pressure rectification zone and. reheating it by heat exchange with said second fraction of the air. t
5. A process according to claim 4, wherein the first fraction of the, air is introduced into the higher pressure column.
6. A process according to claim 5, wherein the gaseous nitrogen is reheated before its expansion with external work by heat exchange with liquid nitrogen extracted in the high pressure rectification zone and sent to the lower.
pressure rectification zone.
7. A process according to claim 5, wherein the gaseous nitrogen is reheated after its expansion with external work,
by heat exchange with a liquid enriched with oxygen originating from the higher pressure rectification zone and sent to the. lower pressure rectification zone.
References Cited in the file of this patent UNITED STATES PATENTS 2,496,380 Crawford Feb. 7, 1950 2,499,043 Voorhees Feb. 28, 1950 2,627,731 Benedict Feb. 10, 1953 2,699,047 Karwat Jan. 11, 1955 2,763,138 Tsunoda Sept. 18, 1956 2,779,174 Vesque Jan. 29, 1957 2,827,775 Linde Mar. 25, 1958 2,873,583 Potts Feb. 17, 1959 FOREIGN PATENTS 1,108,033 France Aug. 17, 1955
Claims (1)
1. IN A PROCESS OF PRODUCTION OF OXYGEN UNDER PRESSURE BY THE LIQUEFACTION AND RECTIFICATION OF AIR IN AT LEAST TWO RECTIFYING ZONES UNDER SUCCESSIVELY LOWER PRESSURES, WHEREIN THE AIR TO BE SEPARATED IS DIVIDED INTO TWO FRACTIONS, THE FIRST ONE OF WHICH IS COMPRESSED TO A HIGHER PRESSURE THAN THE SECOND ONE AND COOLED BY HEAT EXCHANGE WITH LIQUID OXYGEN UNDER PRESSURE, THEN INTRODUCED INTO A RECTIFYING ZONE AND THE SECOND ONE OF WHICH IS INTRODUCED UNDER ITS ORIGINAL PRESSURE INTO A RECTIFYING ZONE, THE IMPROVEMENT OF MAINTAINING A HIGHER THAN ATMOSPHERIC PRESSURE IN THE RECTIFYING ZONE UNDER THE LOWEST PRESSURE, AND EXPANDING WITH EXTERNAL WORK THE WHOLE OF THE SEPARATED NITROGEN FROM SAID LOWEST PRESSURE TO NEARLY ATMOSPHERIC PRESSURE.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US612441A US2918802A (en) | 1956-09-27 | 1956-09-27 | Process of separation of air into its elements |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR1148546D FR1148546A (en) | 1956-09-27 | 1956-02-09 | Process of separating air into its elements |
| US612441A US2918802A (en) | 1956-09-27 | 1956-09-27 | Process of separation of air into its elements |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US2918802A true US2918802A (en) | 1959-12-29 |
Family
ID=24453168
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US612441A Expired - Lifetime US2918802A (en) | 1956-09-27 | 1956-09-27 | Process of separation of air into its elements |
Country Status (2)
| Country | Link |
|---|---|
| US (1) | US2918802A (en) |
| FR (1) | FR1148546A (en) |
Cited By (24)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3059438A (en) * | 1957-05-13 | 1962-10-23 | Air Prod & Chem | Apparatus and method for fractionation of gas |
| US3086371A (en) * | 1957-09-12 | 1963-04-23 | Air Prod & Chem | Fractionation of gaseous mixtures |
| US3100696A (en) * | 1957-07-04 | 1963-08-13 | Linde Eismasch Ag | Method and apparatus for separating gases |
| US3113854A (en) * | 1960-08-25 | 1963-12-10 | Air Prod & Chem | Method and apparatus for separating gaseous mixtures |
| US3129080A (en) * | 1960-09-13 | 1964-04-14 | Philips Corp | Equipment for supplying both air compressed to high pressure and liquid oxygen |
| US3180101A (en) * | 1959-07-20 | 1965-04-27 | Linde Eismasch Ag | Process and apparatus for the production of cold through work-yielding release of pressure |
| US3210947A (en) * | 1961-04-03 | 1965-10-12 | Union Carbide Corp | Process for purifying gaseous streams by rectification |
| US3214925A (en) * | 1960-08-13 | 1965-11-02 | Linde Eismasch Ag | System for gas separation by rectification at low temperatures |
| US3216206A (en) * | 1961-11-29 | 1965-11-09 | Linde Eismasch Ag | Low temperature distillation of normally gaseous substances |
| US3257814A (en) * | 1962-01-05 | 1966-06-28 | Air Liquide | Process for the manufacture of oxygen-enriched air |
| US3261168A (en) * | 1961-11-03 | 1966-07-19 | Petrocarbon Dev Ltd | Separation of oxygen from air |
| US3280574A (en) * | 1960-10-14 | 1966-10-25 | Linde Ag | High pressure pure gas for preventing contamination by low pressure raw gas in reversing regenerators |
| US3375673A (en) * | 1966-06-22 | 1968-04-02 | Hydrocarbon Research Inc | Air separation process employing work expansion of high and low pressure nitrogen |
| US3416323A (en) * | 1966-01-13 | 1968-12-17 | Linde Ag | Low temperature production of highly compressed gaseous and/or liquid oxygen |
| US3447331A (en) * | 1966-06-01 | 1969-06-03 | British Oxygen Co Ltd | Air separation employing waste nitrogen reheated by incoming air in work expansion |
| US3490246A (en) * | 1965-08-20 | 1970-01-20 | Linde Ag | Split pressure low temperature process for the production of gases of moderate purity |
| US3500651A (en) * | 1966-01-13 | 1970-03-17 | Linde Ag | Production of high pressure gaseous oxygen by low temperature rectification of air |
| US3699695A (en) * | 1965-10-29 | 1972-10-24 | Linde Ag | Process of separating air into an oxygen-rich fraction suitable for blast furnace operation |
| US3754406A (en) * | 1970-03-16 | 1973-08-28 | Air Prod & Chem | The production of oxygen |
| US3798917A (en) * | 1970-05-12 | 1974-03-26 | Messer Griesheim Gmbh | Fractionation of air to obtain oxygen of about seventy percent purity |
| US4022030A (en) * | 1971-02-01 | 1977-05-10 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Thermal cycle for the compression of a fluid by the expansion of another fluid |
| US4133662A (en) * | 1975-12-19 | 1979-01-09 | Linde Aktiengesellschaft | Production of high pressure oxygen |
| US5165244A (en) * | 1991-05-14 | 1992-11-24 | Air Products And Chemicals, Inc. | Process to produce oxygen and nitrogen at medium pressure |
| US5515688A (en) * | 1993-02-25 | 1996-05-14 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for the production of oxygen and/or nitrogen under pressure |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2461906A1 (en) * | 1979-07-20 | 1981-02-06 | Air Liquide | Cryogenic air separation method and installation with oxygen production at high pressure |
| GB2080929B (en) * | 1980-07-22 | 1984-02-08 | Air Prod & Chem | Producing gaseous oxygen |
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| US2496380A (en) * | 1946-04-18 | 1950-02-07 | Elliott Co | Gas purifying method and apparatus |
| US2499043A (en) * | 1947-03-26 | 1950-02-28 | Standard Oil Co | Heat exchange |
| US2627731A (en) * | 1949-06-18 | 1953-02-10 | Hydrocarbon Research Inc | Rectification of gaseous mixtures |
| US2699047A (en) * | 1950-10-27 | 1955-01-11 | Linde Eismasch Ag | Process for cooling and purifying compressed gas mixtures |
| FR1108033A (en) * | 1954-06-29 | 1956-01-09 | Air Liquide | A method of cooling separation of gaseous mixtures comprising at least three components |
| US2763138A (en) * | 1954-02-16 | 1956-09-18 | American Messer Corp | Process and apparatus for separating gases |
| US2827775A (en) * | 1949-11-11 | 1958-03-25 | Linde Eismasch Ag | Process for separating a compressed gas mixture |
| US2873583A (en) * | 1954-05-04 | 1959-02-17 | Union Carbide Corp | Dual pressure cycle for air separation |
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| US2496380A (en) * | 1946-04-18 | 1950-02-07 | Elliott Co | Gas purifying method and apparatus |
| US2499043A (en) * | 1947-03-26 | 1950-02-28 | Standard Oil Co | Heat exchange |
| US2627731A (en) * | 1949-06-18 | 1953-02-10 | Hydrocarbon Research Inc | Rectification of gaseous mixtures |
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| US2763138A (en) * | 1954-02-16 | 1956-09-18 | American Messer Corp | Process and apparatus for separating gases |
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Cited By (24)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3059438A (en) * | 1957-05-13 | 1962-10-23 | Air Prod & Chem | Apparatus and method for fractionation of gas |
| US3100696A (en) * | 1957-07-04 | 1963-08-13 | Linde Eismasch Ag | Method and apparatus for separating gases |
| US3086371A (en) * | 1957-09-12 | 1963-04-23 | Air Prod & Chem | Fractionation of gaseous mixtures |
| US3180101A (en) * | 1959-07-20 | 1965-04-27 | Linde Eismasch Ag | Process and apparatus for the production of cold through work-yielding release of pressure |
| US3214925A (en) * | 1960-08-13 | 1965-11-02 | Linde Eismasch Ag | System for gas separation by rectification at low temperatures |
| US3113854A (en) * | 1960-08-25 | 1963-12-10 | Air Prod & Chem | Method and apparatus for separating gaseous mixtures |
| US3129080A (en) * | 1960-09-13 | 1964-04-14 | Philips Corp | Equipment for supplying both air compressed to high pressure and liquid oxygen |
| US3280574A (en) * | 1960-10-14 | 1966-10-25 | Linde Ag | High pressure pure gas for preventing contamination by low pressure raw gas in reversing regenerators |
| US3210947A (en) * | 1961-04-03 | 1965-10-12 | Union Carbide Corp | Process for purifying gaseous streams by rectification |
| US3261168A (en) * | 1961-11-03 | 1966-07-19 | Petrocarbon Dev Ltd | Separation of oxygen from air |
| US3216206A (en) * | 1961-11-29 | 1965-11-09 | Linde Eismasch Ag | Low temperature distillation of normally gaseous substances |
| US3257814A (en) * | 1962-01-05 | 1966-06-28 | Air Liquide | Process for the manufacture of oxygen-enriched air |
| US3490246A (en) * | 1965-08-20 | 1970-01-20 | Linde Ag | Split pressure low temperature process for the production of gases of moderate purity |
| US3699695A (en) * | 1965-10-29 | 1972-10-24 | Linde Ag | Process of separating air into an oxygen-rich fraction suitable for blast furnace operation |
| US3416323A (en) * | 1966-01-13 | 1968-12-17 | Linde Ag | Low temperature production of highly compressed gaseous and/or liquid oxygen |
| US3500651A (en) * | 1966-01-13 | 1970-03-17 | Linde Ag | Production of high pressure gaseous oxygen by low temperature rectification of air |
| US3447331A (en) * | 1966-06-01 | 1969-06-03 | British Oxygen Co Ltd | Air separation employing waste nitrogen reheated by incoming air in work expansion |
| US3375673A (en) * | 1966-06-22 | 1968-04-02 | Hydrocarbon Research Inc | Air separation process employing work expansion of high and low pressure nitrogen |
| US3754406A (en) * | 1970-03-16 | 1973-08-28 | Air Prod & Chem | The production of oxygen |
| US3798917A (en) * | 1970-05-12 | 1974-03-26 | Messer Griesheim Gmbh | Fractionation of air to obtain oxygen of about seventy percent purity |
| US4022030A (en) * | 1971-02-01 | 1977-05-10 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Thermal cycle for the compression of a fluid by the expansion of another fluid |
| US4133662A (en) * | 1975-12-19 | 1979-01-09 | Linde Aktiengesellschaft | Production of high pressure oxygen |
| US5165244A (en) * | 1991-05-14 | 1992-11-24 | Air Products And Chemicals, Inc. | Process to produce oxygen and nitrogen at medium pressure |
| US5515688A (en) * | 1993-02-25 | 1996-05-14 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for the production of oxygen and/or nitrogen under pressure |
Also Published As
| Publication number | Publication date |
|---|---|
| FR1148546A (en) | 1957-12-11 |
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