Cryogenic rectification system for producing ultra high purity oxygen

Abstract
A cryogenic rectification system comprising an upstream krypton/xenon knockout column and a downstream oxygen upgrader column wherein the knockout column processes a crude feed for removal of heavy components including hydrocarbons and the upgrader column produces ultra high purity oxygen.
Description




TECHNICAL FIELD




This invention relates generally to cryogenic rectification and, more particularly, to the use of cryogenic rectification to produce ultra high purity oxygen.




BACKGROUND ART




Ultra high purity oxygen is required in manufacturing processes that are very sensitive to contaminants, such as in the production of semiconductors and other electronic components. As the demand for ultra high purity oxygen increases, there is a need for a system which can efficiently produce ultra high purity oxygen.




Accordingly, it is an object of this invention to provide an improved system for producing ultra high purity oxygen.




SUMMARY OF THE INVENTION




The above and other objects, which will become apparent to those skilled in the art upon a reading of this disclosure, are attained by the present invention, one aspect of which is:




A method for producing ultra high purity oxygen by cryogenic rectification comprising:




(A) providing a feed comprising oxygen, argon, krypton and xenon, and passing the feed into the upper portion of a first column;




(B) separating the feed by cryogenic rectification within the first column into a top fluid comprising oxygen and argon, and into a bottom fluid comprising krypton and xenon;




(C) passing top fluid from the upper portion of the first column into the upper portion of a second column, and separating the top fluid by cryogenic rectification within the second column into argon-enriched fluid and ultra high purity oxygen; and




(D) withdrawing ultra high purity oxygen from the lower portion of the second column and recovering the withdrawn ultra high purity oxygen as product.




Another aspect of the invention is:




Apparatus for producing ultra high purity oxygen comprising:




(A) a first column having a top condenser and a bottom reboiler, and means for passing a feed comprising oxygen, argon, krypton and xenon into the upper portion of the first column;




(B) a second column having a top condenser and a bottom reboiler, and means for passing fluid from the upper portion of the first column into the upper portion of the second column;




(C) means for passing fluid from the bottom reboiler of the first column to the top condenser of the first column, and means for passing fluid from the bottom reboiler of the second column to the top condenser of the second column; and




(D) means for recovering ultra high purity oxygen from the lower portion of the second column.




As used herein the term “ultra high purity oxygen” means a fluid having an oxygen concentration of at least 99.99 mole percent.




As used herein the term “column” means a distillation or fractionation column or zone, i.e. a contacting column or zone, wherein liquid and vapor phases are countercurrently contacted to effect separation of a fluid mixture, as for example, by contacting of the vapor and liquid phases on a series of vertically spaced trays or plates mounted within the column and/or on packing elements such as structured or random packing. For a further discussion of distillation columns, see the Chemical Engineer's Handbook, fifth edition, edited by R. H. Perry and C. H. Chilton, McGraw-Hill Book Company, New York, Section 13,


The Continuous Distillation Process.






Vapor and liquid contacting separation processes depend on the difference in vapor pressures for the components. The high vapor pressure (or more volatile or low boiling) component will tend to concentrate in the vapor phase whereas the low vapor pressure (or less volatile or high boiling) component will tend to concentrate in the liquid phase. Distillation is the separation process whereby heating of a liquid mixture can be used to concentrate the more volatile component(s) in the vapor phase and thereby the less volatile component(s) in the liquid phase. Partial condensation is the separation process whereby cooling of a vapor mixture can be used to concentrate the volatile component(s) in the vapor phase and thereby the less volatile component(s) in the liquid phase. Rectification, or continuous distillation, is the process that combines successive partial vaporizations and condensations as obtained by a countercurrent treatment of the vapor and liquid phases. The countercurrent contacting of the vapor and liquid phases can be adiabatic or nonadiabatic and can include integral (stagewise) or differential (continuous) contact between the phases. Separation process arrangements that utilize the principles of rectification to separate mixtures are often interchangeably termed rectification columns, distillation columns, or fractionation columns. Cryogenic rectification is a rectification process carried out at least in part at temperatures at or below 150 degrees Kelvin (K).




As used herein, the term “indirect heat exchange” means the bringing of two fluids into heat exchange relation without any physical contact or intermixing of the fluids with each other.




As used herein, the term “upper portion” and “lower portion” mean those sections of a column respectively above and below the mid point of the column.




As used herein, the term “tray” means a contacting stage, which is not necessarily an equilibrium stage, and may mean other contacting apparatus such as packing having a separation capability equivalent to one tray.




As used herein, the term “equilibrium stage” means a vapor-liquid contacting stage whereby the vapor and liquid leaving the stage are in mass transfer equilibrium, e.g. a tray having 100 percent efficiency or a packing element height equivalent to one theoretical plate (HETP).




As used herein, the term “top” when referring to a column means that section of the column above the column mass transfer internals, i.e. trays or packing.




As used herein, the term “bottom” when referring to a column means that section of the column below the column mass transfer internals, i.e. trays or packing.




As used herein, the term “bottom reboiler” means a heat exchanger for generating column upflow vapor from column liquid.




As used herein, the term “top condenser” means a heat exchanger for generating column downflow liquid from column vapor.











BRIEF DESCRIPTION OF THE DRAWINGS





FIG. 1

is a schematic representation of one preferred embodiment of the ultra high purity oxygen production system of this invention.





FIG. 2

is a schematic representation of another preferred embodiment of the ultra high purity oxygen production system of this invention.











The numerals in the Drawings are the same for the common elements.




DETAILED DESCRIPTION




The invention will be described in detail with reference to the Drawings.




Referring now to

FIG. 1

, feed stream


101


is passed into the upper portion of first column


100


, which is operating at a pressure generally within the range of from 15 to 50 pounds per square inch absolute (psia). Stream


101


may be liquid, gaseous or mixed phase. Typically stream


101


is taken from a cryogenic air separation plant such as a single column nitrogen plant, a double column plant producing oxygen or both nitrogen and oxygen, or a triple column plant producing argon in addition to oxygen and nitrogen.




Feed


101


comprises oxygen, argon, krypton and xenon. Generally feed


101


has an oxygen concentration within the range of from 98 to 99.9 mole percent. Because the product of this invention is ultra high purity oxygen, it is imperative that the presence of flammables such as hydrocarbons be minimized in the process. It is preferred in the practice of this invention that feed


101


undergo hydrocarbon removal prior to passage into first column


100


. In one preferred hydrocarbon removal procedure, the hydrocarbons are removed by heating the feed to about 1000° F. and passing the heated feed over a rare earth catalyst such as platinum. The hydrocarbons will combine with oxygen in the feed and be converted to carbon dioxide and water. The resulting feed which is now substantially free of hydrocarbons is cooled and passed through a molecular sieve dryer to remove the carbon dioxide and water and then further cooled, preferably to just above its saturation point, prior to passage into first column


100


.




Feed


101


preferably is passed into first column


100


at a level from 20 to 30 equilibrium stages below the top of column


100


. Within first column


100


, feed


101


is separated by cryogenic rectification into a top fluid comprising oxygen and argon and into a bottom fluid which contains most of the krypton and xenon which was in feed


101


.




First column


100


has top condenser


150


and bottom reboiler


160


. Bottom reboiler


160


is driven by vapor


110


, such as oxygen, which is condensed in reboiler


160


by indirect heat exchange with the bottom fluid to provide vapor upflow for the column. Preferably vapor


110


is from the cryogenic air separation system from which feed stream


101


is taken. The resulting condensed reboiler driving fluid


111


is throttled through valve


35


and then passed into top condenser


150


as stream


107


. If necessary, additional liquid


114


may be passed into top condenser


150


to ensure that sufficient refrigeration is supplied to top condenser


150


to adequately reflux first column


100


. Bottom liquid, having a higher concentration of krypton and/or xenon as a result of the reboiling, is withdrawn from the system in stream


109


. Typically the bottom fluid in stream


109


will have a krypton and xenon concentration of at least 90 mole percent. Stream


109


may contain a small fraction of oxygen, generally from 1 to 10 mole percent, as well as trace amounts of other components having boiling points higher than oxygen.




Top fluid is withdrawn from the upper portion of the first column and passed into the upper portion of a second column. In the embodiment of the invention illustrated in

FIG. 1

, top fluid comprising oxygen and argon is withdrawn from the top of first column


100


in vapor stream


102


which is passed into top condenser


150


. Within top condenser


150


top fluid


102


is condensed by indirect heat exchange with driving fluid


107


which is at least partially vaporized and withdrawn from the system in stream


108


. Resulting condensed top fluid


103


from top condenser


150


is passed as reflux stream


104


back into first column


100


, and as stream


105


into the upper portion of second column


200


as was previously described. Preferably feed stream


105


containing oxygen and argon is passed into second column


200


at a level from 3 to 40 equilibrium stages below the top of second column


200


. Top condenser


150


is operated in such a manner to ensure that any hydrocarbons that may be in feed stream


101


are washed down the column by the downflowing reflux and removed from the system in stream


109


, thereby enabling the feed to the second column to be essentially free of any hydrocarbons.




Second or upgrader column


200


is operating at a pressure generally within the range of from 15 to 50 psia. Within second column


200


the top fluid passed into this column from first column


100


is separated by cryogenic rectification into argon-enriched fluid and ultra high purity oxygen.




Second column


200


has a top condenser


250


and a bottom reboiler


260


. Bottom reboiler


260


is driven by vapor


210


such as nitrogen, which is condensed in reboiler


260


by indirect heat exchange with ultra high purity oxygen liquid at the bottom of second column


200


, serving to boil a portion of this liquid to provide vapor upflow for the column and in the process increasing the oxygen concentration of the ultra high purity oxygen liquid. Preferably vapor


210


is taken from the air separation system from which feed


101


is taken. The resulting condensed reboiler driving fluid


211


is throttled through valve


36


and then passed into top condenser


250


as stream


207


. If necessary, additional liquid


212


may be passed into top condenser


250


to ensure that sufficient refrigeration is supplied to top condenser


250


to reflux second column


200


. Ultra high purity oxygen bottom liquid, having a higher concentration of oxygen as a result of the reboiling, is withdrawn from the lower portion of second column


200


in stream


209


and recovered as product ultra high purity oxygen. If desired, in addition to or in place of liquid stream


209


, ultra high purity oxygen may be recovered from second column


200


from above bottom reboiler


260


as shown by stream


38


.




Argon-enriched fluid is withdrawn from the upper portion of second column


200


in vapor stream


201


and a portion


204


is removed from the system as an overhead waste stream. Another portion


202


is passed into top condenser


250


wherein it is condensed by indirect heat exchange with driving fluid


207


which is at least partially vaporized and removed from the system in stream


208


. Resulting condensed argon-enriched fluid


203


from top condenser


25


is passed back into the upper portion of second column


200


as reflux.





FIG. 2

illustrates another embodiment of the invention. The elements of the embodiment illustrated in

FIG. 2

which are common with those elements of the embodiment illustrated in

FIG. 1

will not be described again in detail. Referring now to

FIG. 2

, top fluid stream


102


is divided into portion


112


, which is removed from the system, and into portion


106


which is passed into top condenser


150


for condensation to produce reflux liquid


103


which is passed back into first column


100


in its entirety. In the embodiment of the invention illustrated in

FIG. 2

, the top fluid for passage into the upper portion of the second column is taken directly from the upper portion of first column


100


as stream


37


without first going through the top condenser as in the embodiment illustrated in FIG.


1


. An oxygen stream


113


, having an oxygen concentration generally within the range of from 99 to 99.99 mole percent, is withdrawn from the upper portion of first column


100


, but from a level at least one equilibrium stage below the withdrawal level of the top fluid, e.g., stream


37


. Oxygen stream


113


may be recovered as product or may be passed on to another column for further processing.




In the embodiment of the invention illustrated in

FIG. 2

, vaporized first column top condenser driving fluid


108


is not directly removed from the system but instead is passed into second column bottom reboiler


260


wherein it is condensed by indirect heat exchange with ultra high purity oxygen liquid and then passed on to top condenser


250


as was previously described.




Although the invention has been described in detail with reference to certain preferred embodiments, those skilled in the art will recognize that there are other embodiments of the invention within the spirit and the scope of the claims.



Claims
  • 1. A method for producing ultra high purity oxygen by cryogenic rectification comprising:(A) providing a feed comprising oxygen, argon, krypton and xenon, and passing the feed into the upper portion of a first column; (B) separating the feed by cryogenic rectification within the first column into a top fluid comprising oxygen and argon, and into a bottom fluid comprising krypton and xenon; (C) passing top fluid from the upper portion of the first column into the upper portion of a second column, and separating the top fluid by cryogenic rectification within the second column into argon-enriched fluid and ultra high purity oxygen; and (D) withdrawing ultra high purity oxygen from the lower portion of the second column and recovering the withdrawn ultra high purity oxygen as product.
  • 2. The method of claim 1 wherein at least some of the ultra high purity oxygen product is recovered as liquid.
  • 3. The method of claim 1 wherein the bottom fluid has a krypton and xenon concentration of at least 90 mole percent.
  • 4. The method of claim 1 wherein the feed has an oxygen concentration within the range of from 98 to 99.9 mole percent.
  • 5. The method of claim 1 wherein the feed undergoes a hydrocarbon removal procedure prior to being passed into the first column.
  • 6. The method of claim 5 wherein the hydrocarbon removal procedure comprises heating the feed, passing the heated feed over a rare earth catalyst, cooling the feed, and passing the cooled feed through a molecular sieve dryer.
  • 7. Apparatus for producing ultra high purity oxygen comprising:(A) a first column having a top condenser and a bottom reboiler, and means for passing a feed comprising oxygen, argon, krypton and xenon into the upper portion of the first column; (B) a second column having a top condenser and a bottom reboiler, and means for passing fluid from the upper portion of the first column into the upper portion of the second column; (C) means for passing fluid from the bottom reboiler of the first column to the top condenser of the first column, and means for passing fluid from the bottom reboiler of the second column to the top condenser of the second column; and (D) means for recovering ultra high purity oxygen from the lower portion of the second column.
  • 8. The apparatus of claim 7 wherein the means for passing fluid from the upper portion of the first column into the upper portion of the second column includes the top condenser of the first column.
  • 9. The apparatus of claim 7 further comprising means for passing fluid from the top condenser of the first column to the bottom reboiler of the second column.
  • 10. The apparatus of claim 7 further comprising means for recovering fluid from the bottom of the first column.
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