Cryogenic process for producing ultra high purity nitrogen

Abstract: Ultra high purity, e.g., nitrogen having less than 0.1 ppm of light impurities is generated with enhanced nitrogen in a cryogenic process for the separation of air utilizing an integrated multi-column distillation system comprising a first column (102) and an ultra high purity nitrogen column (104) by withdrawing liquid nitrogen from the first column, charging that fraction (20) as feed to the ultra high purity nitrogen column, withdrawing a nitrogen stream (14) which is rich in volatile contaminants from the top of the first column, partially condensing (in 108) that nitrogen stream, removing the uncondensed portion (18) which has been concentrated in volatile contaminants as a purge stream, and returning the condensed portion (16) to the distillation system as reflux.

Description: This invention relates to a cryogenic process for the separation of air and recovering ultra high purity nitrogen with high nitrogen recovery. Numerous process are known for the separation of air by cryogenic distillation into its constituent components. Typically, the air separation process involves removal of contaminant materials such as carbon dioxide and water from a compressed air stream prior to cooling to near its dew point. The cooled air then is cryogenically distilled in an integrated multi-column distillation system. Processes to produce a high purity nitrogen stream containing few light contaminants, such as hydrogen, helium and neon have been proposed. Concentration of some of these contaminants in the feed air can be as high as 20 ppm. Almost all of these light components show up in the final nitrogen product from an air separation unit (ASU). In some cases, such as for the electronics industry, this contamination level is unacceptable in the end use of this nitrogen product. The following patents disclose approaches to the problem. US-A-4,824,453 discloses a process for producing ultra high purity oxygen as well as high purity nitrogen, where the nitrogen purity exceeds 99.998% and the amount of impurities is generally less than 10 ppm. More specifically, air is compressed, cooled and distilled in a rectification system wherein in a first stage rectification an oxygen enriched fraction is removed from the bottom and a nitrogen rich liquid fraction is removed from an upper portion of the first stage rectification, sub-cooled and returned as reflux to the top of the second stage rectification. A nitrogen rich liquid is removed from an upper portion of the second stage at a point just below an overhead removal point for nitrogen vapor from the second stage rectification. Liquid oxygen from the bottom of the first stage is sub-cooled, expanded and used to drive a boiler/condenser in the top of the high purity argon column. Nitrogen vapor from the top of the first stage is used to drive a reboiler/condenser in the bottom of a high purity oxygen column. To enhance product purity, a portion of the gaseous nitrogen stream from the top of the first column is removed as purge. US-A-4,902.321 discloses a process for producing ultra high purity nitrogen in a multi-column system. Air is compressed, cooled and charged to a first column where it is separated into its own components generating an oxygen liquid at the bottom and a nitrogen rich vapour at the top. The oxygen liquid is expanded and used to drive a boiler/condenser which is thermally linked to the top of the first column for condensing the nitrogen rich vapor. A portion of the nitrogen rich vaoor is removed from the top of the first column and condensed in the tube side of a heat exchanger. The resulting liquid nitrogen is expanded and charged to a the top of a stripping column wherein nitrogen including impurities are flashed from the stripping column. Any impurities not removed by flashing are stripped by passing a stream of substantially pure nitrogen upwardly through the column. The nitrogen liquid collected at the bottom of the stripping column is pumped to the shell side of the heat exchanger, vaporized against the nitrogen-rich vapor and removed as high purity product. EP-A-0 0376465 discloses an air separation process for producing ultra high purity nitrogen product. In the process, nitrogen product from a conventional air separation process is charged to the bottom of a column equipped with a reflux condenser. Liquid nitrogen is withdrawn from an upper portion of the column and flashed generating a liquid and a vapor. The liquid obtained after flashing is then flashed a second time and the resulting liquid recovered. CA-A-2,048 146 discloses a process, which can be utilized to reduce volatile contaminants in a crude liquid nitrogen stream from the high pressure column of a dual column system, by charging the crude liquid nitrogen to the top of a third distillation column. In this third distillation column, the crude liquid nitrogen stream is stripped of volatile impurities by ascending vapor. The overhead from the third column may be returned to an upper portion of the high pressure column and the liquid bottoms is fed to the low pressure column. EP-A-0 485 612 discloses a process in which air is separated in a higher pressure (HP) column into nitrogen rich overhead, intermediate liquid nitrogen stream and bottoms liquid. The overhead is (apparently) partially condensed and the condensed portion returned as reflux to the HP column. An (apparently) uncondensed portion of the overhead vapour is removed as a helium-rich stream. The liquid nitrogen stream is reduced in pressure and fed to an intermediate location of an ultra high purity ("UHPN") column providing UHPN product . The UHPN column overhead is (apparently) partially condensed ; the condensed fraction returned to the UHPN column as reflux and the (apparently) uncondensed portion is removed as a helium-rich stream. Boil-up to the UHPN column is provided by heat-exchange with nitrogen overhead from the HP column. There are essentially two problems associated with the processes described for producing ultra-high purity nitrogen and these problems relate to the fact that in the '453 process purities are quite often not sufficiently high to meet industry specifications and in the '321 process nitrogen recoveries are too low. The same can be said of the '465 European patent process. This invention relates to a process for producing an ultra high purity nitrogen product by the cryogenic separation, in an integrated multi-column distillation system comprising a first distillation column and an ultra high purity nitrogen distillation column, of air comprising volatile impurities, wherein an air stream is compressed, freed of condensible impurities, and cooled generating a feed for the integrated multi-column distillation system, said process comprising : a) generating a nitrogen rich vapour containing volatile impurities in an upper part of the first column and a crude liquid oxygen fraction in a lower part of said first column ; b) removing at least a fraction of said nitrogen-rich vapour containing volatile impurities and partially condensing at least a portion of said stream thereby forming a first condensed fraction and an uncondensed fraction ; c) returning at least a portion of said first condensed fraction as reflux to the first column in the distillation system; d) removing at least a portion of the uncondensed nitrogen rich vapour fraction rich in volatile impurities generated in step b) as a purge stream; e) generating a liquid nitrogen fraction in an upper part of said first column and removing said liquid nitrogen fraction from the first column at a location at or below that at which said nitrogen rich vapour is removed; f) introducing the liquid nitrogen fraction to an upper part of the ultra high purity nitrogen column as feed, said column operating at the same pressure as the first column ; g) generating a nitrogen rich vapour fraction containing residual volatile impurities in the ultra high purity nitrogen column, removing that fraction as an overhead and returning the fraction to the first column; and h) removing an ultra high purity nitrogen fraction from the ultra high purity nitrogen column, wherein said ultra high purity nitrogen fraction is expanded and warmed against a fraction of the nitrogen rich vapour containing volatile impurities from the first column in a boiler/condenser thereby at least partially condensing a fraction of the nitrogen rich vapour, separating the condensed fraction from any uncondensed vapour fraction, and returning the condensed fraction to the first distillation column or the ultra high purity distillation column. This invention also relates to an integrated multi-column distillation system comprising a first distillation column and an ultra high purity nitrogen distillation column for producing an ultra high purity nitrogen product by the cryogenic separation of air comprising volatile impurities by the process of the invention, the system comprising: means for producing a cold, compressed air feed free of condensible impurities and feeding same to the first column; condensing means for partially condensing at least a portion of a fraction of nitrogen-rich vapour containing volatile impurities removed from an upper part of the first column to form a first condensed fraction and an uncondensed fraction; conduit means for returning at least a portion of said first condensed fraction as reflux to the first column in the distillation system; conduit means for removing at least a portion of said uncondensed nitrogen as a purge stream; conduit means for introducing as feed a liquid nitrogen fraction from an upper part of the first column at a location at or below that at which said nitrogen rich, vapour is removed to an upper part of the ultra high purity nitrogen column; conduit means for removing as overhead a nitrogen rich vapour fraction containing residual volatile impurities from the ultra high purity nitrogen column and returning said fraction to the first column at the same pressure; conduit means for removing an ultra high purity nitrogen fraction from the ultra high purity nitrogen column; and a boiler/condenser for expanding the liquid nitrogen removed by the conduit means and warming it against a fraction of the nitrogen rich vapour containing volatile impurities from the first column thereby at least partially condensing a fraction of the nitrogen rich vapour. There are several advantages associated with this process, those being the ability to produce nitrogen via a standard nitrogen generator plant with the resultant nitrogen being of ultra high purity and with high recovery of nitrogen based on feed air introduced to the process. The following is a description by way of example only and with reference to the accompanying drawings of presently preferred embodiments of the present invention. In the drawings:- Figure 1 is a schematic representation of an embodiment for generating ultra high purity nitrogen with enhanced nitrogen recovery. Figure 2 is a schematic representation of an embodiment wherein nitrogen rich vapor and liquid are removed from the same location of the upper part of the first column. Figure 3 is a schematic representation of an embodiment for producing ultra high purity nitrogen employing the removal of a single purge. To facilitate an understanding of the invention and the concepts for generating in ultra high purity nitrogen product having a volatile impurity content of less than 5 ppm and preferably less than 0.1 ppm, reference is made to the embodiment shown in Figure 1. More particularly, a feed air stream 10 is initially prepared from an air stream by compressing an air stream comprising oxygen, nitrogen, argon, volatile impurities such as hydrogen, neon, and helium and condensible impurities, such as, carbon dioxide and water in a multi-stage compressor system (MAC) to a pressure ranging from 70 to 300 psia (480 to 2070 kPa). Volatile impurities have a much lower boiling point than nitrogen. This compressed air stream is cooled with cooling water and chilled against a refrigerant and then passed through a molecular sieve bed to free it of condensible water and carbon dioxide impurities. The integrated multi-column distillation system comprises a first column 102 and an ultra high purity nitrogen column 104. Both columns 102 and 104 are operated at the same pressures and pressures which are close in pressure to that of the feed air stream 10, e.g. 70 to 300 psia (480 to 2070 kPa), and typically from 90-150 psia (620 to 1040 kPa). Air is separated into its components by intimate contact of the vapor and liquid in the first column 102. which is equipped with distillation trays or packing, either medium being suited for effecting liquid/vapor contact. A nitrogen vapor stream containing a high concentration of volatile impurities is generated at the top portion of first column 102 and a crude liquid oxygen stream is generated at the bottom of first column 102. In the process an air stream 10 free of condensible impurities is cooled to near its dew point in main heat exchanger system 100. The air stream then forms the feed via stream 12 to first column 102 associated with the integrated multi-column distillation system. A nitrogen rich vapor containing volatile impurities is generated as an overhead and a crude liquid oxygen fraction as a bottoms fraction. At least a portion of the nitrogen vapor generated in first column is withdrawn via line 14 and partially condensed in boiler/condenser 108 located at the top of first column 102. Condensation of the nitrogen rich vapor containing light impurities concentrates these impurities in the uncondensed vapor phase. The condensed nitrogen, which has a fractional amount of impurities, is withdrawn from boiler/condenser 108 and at least a portion directed to the top of first column 102 as reflux via line 16. The uncondensed nitrogen vapor containing a large portion of the impurities is removed via line 18 as a purge. In this embodiment a liquid nitrogen fraction is collected in an upper part of the first column, preferably at a point typically about 2-5 trays below the nitrogen removal point via line 14 in first column 102. That liquid nitrogen fraction is removed via line 20 and introduced to the top of ultra high purity nitrogen column 104 as feed and reflux. Ultra high purity nitrogen column 104 is operated within a pressure range from 70-300 (480 to 2070 kPa), typically 90-150 psia (620 to 1040 kPa), in order to produce an ultra high purity nitrogen product. The objective in the ultra high purity nitrogen column is to provide ultra high purity nitrogen, e.g., greater than 99.998% preferably 99.999% by volume purity at the bottom of the column. Ultra high purity nitrogen column 104 is equipped with vapor liquid contact medium which comprises distillation trays or packing. It is in ultra high purity nitrogen column 104 where ultra high purity nitrogen is generated. The key to its success is the ultimate concentration and removal of a large part of the volatile impurities from a nitrogen vapor. More particularly, a nitrogen-rich stream containing residual volatile impurities is generated and removed from the top or uppermost portion of ultra high purity nitrogen column 104 as an overhead via line 32 wherein it is returned to the upper to middle portion of first column impurities. The concentration of residual volatile impurities in nitrogen vapor stream 32 is primarily controlled by the purge nitrogen stream removed from an upper portion of first column 102 as this governs the amount of volatile submitted to the ultra high purity nitrogen column. An ultra high purity nitrogen product is generated as a liquid fraction (LIN) in the bottom portion of the ultra high purity nitrogen column 104 and removed via line 34. The ultra high purity liquid nitrogen (stream 34) is vaporized by feeding it to a boiler/condenser 114 therein. The liquid stream is expanded through a valve and charged to the vaporizer side of the boiler/condenser 114. This vaporization of the liquid nitrogen at least partially condenses the nitrogen rich stream containing volatiles taken as an overhead from first column 102 via line 35. An ultra high purity nitrogen product is obtained as a liquid fraction from the boiler/condenser via line 38 and as a vapor fraction via line 40. The condensed fraction is returned to the first column 102 as reflux via line 37. If the nitrogen feed containing volatiles in line 35 is partially condensed in boiler/condenser 114, then the uncondensed portion is removed as a purge stream via line 41. This purge stream may be combined with purge stream 18 and discarded. Alternatively, the purge streams may be collected for the recovery of light contaminants helium, hydrogen and neon. Oxygen is not a desired product in this nitrogen generating process. Crude liquid oxygen is removed from first column 102 as a bottoms fraction via line 42, cooled in boiler/condenser 110, expanded and then charged via line 43 to the vaporizer section of boiler/condenser 108 located at the top of first column 102. The vaporized portion of the oxygen is removed via line 44 as an overhead and the balance as a liquid purge via line 45. Some of the overhead is diverted to a turboexpander 116 via line 46 with the balance being warmed in main heat exchanger 100 and then diverted to turboexpander 116. The exhaust from turboexpander 116 is warmed against process fluids in heat exchanger 100 and the discharged as waste. Optionally, a small fraction of the feed to turboexpander 116 may be diverted through an expansion valve and then discharged as waste. Boilup at the bottom of the ultra high purity nitrogen column 104 is provided by cooling crude liquid oxygen 42 in the boiler/condenser 110. Alternatively. this boilup can be achieved bv heat exchanqe with any suitable fluid. An example can be condensation of a portion of the feed air stream 12 in the boiler/condenser 110 to provide the boilup at the bottom of the ultra high purity nitrogen column 104. In this case, the condensed air stream will be returned to a suitable location in the first distillation column 102. Also, it is possible to use more than one fluid for heat exchange in the bottom boiler/condenser 110. In Figure 1, two purge streams 18 and 41 rich in light volatile impurities are shown, one from boiler/condenser 108 and one from boiler/condenser 114. However, it is not totally necessary to take purge from both of these boiler/condensers and any nitrogen rich stream containing volatiles may be totally condensed in any one of them. A purge stream from at least one of the boiler/condensers 108 or 114 is necessary but purge from both as shown Figure 1 will decrease the concentration of volatiles in the feed to the ultra high purity nitrogen column 104. Further discussion of this feature is provided with respect to the description of the process shown in Fig. 3. Even though not shown in Figure 1, it is also possible to withdraw an ultra high purity gaseous nitrogen stream as product from the bottom of the ultra high purity nitrogen column 104. This route will be more attractive when only a fraction of the total nitrogen product is needed as an ultra high purity gaseous nitrogen. In such a case, most of the nitrogen product will be produced of standard purity from the top section of the first distillation column 102 and a gaseous ultra high purity nitrogen product from the bottom of the ultra high purity nitrogen column 104. The pressure of both the nitrogen products will be nearly identical. Figure 2 provides a variation on the embodiment shown in Figure 1. Equipment numbers utilized in Figure 1 are utilized for the equipment in Figure 2; line numbers have been renumbered using a 200 series. By and large the basic difference between the process of Figure 1 and Figure 2 is that the vapor fraction and liquid fraction are withdrawn from an upper portion of first column 102 at essentially the same location of the first column. Such process results in higher levels of impurities to be carried over with the nitrogen rich vapor fraction containing low boiling light volatile contaminants and with the liquid nitrogen from first column 102. By eliminating the trays in the upper part of the column, which trays were shown in Figure 1, equipment costs can be reduced by eliminating the need for separate means to distribute reflux from boiler/condenser 108 and boiler/condenser 114 to the first column. Also by elimination of trays in the upper part of first column 102, one eliminates the associated pressure drop, although minimal, associated with such trays. More specifically, the embodiment of Figure 2 shows the removal of a nitrogen rich vapor stream containing light volatile contaminants via line 235 from first column 102 at a point above the trays in first column 102. As in the process described in Figure 1 this stream is partially condensed in boiler/condenser 114 with the condensed fraction being returned via line 237 and the uncondensed fraction removed as a purge via line 241. However, the condensed nitrogen stream in line 237 is directly fed to the ultra high purity nitrogen column 104 and the feed stream 220 is only a small liquid stream withdrawn from the top of the first column 102. This is equivalent to the withdrawal of a large liquid nitrogen stream 220 from the first column 102 and forming only a single feed to ultra high purity column 104. Because of the increased concentration of light volatile impurities in the liquid feed to the ultra high purity column 104, either a higher boilup or greater number of theoretical stages of separation would be needed in this column for the same production rate of the ultra high purity nitrogen. All other functions of the process in Figure 2 are similar to those functions described in the operation of process of Figure 1 even though the 200 series of numbers is used. Figure 3 illustrates a variation of the embodiment of Figure 1. Equipment designations used in Figure 1 are used in Figure 3 and stream functions have been designated using a 300 series to differentiate the process from Figure 1. The embodiment in Figure 3 utilizes a first column of similar design to that of Figure 1 and it contains a major separation section followed by a top refining section for further concentration of the light volatile contaminants in the overhead fraction. In contrast to Figure 1, the nitrogen rich stream containing volatile contaminants is removed via line 335 in an upper part of the first column at a point below the top refining section and charged to boiler/condenser 114. Substantially all of the nitrogen overhead fraction is condensed in boiler/condenser 114 and the condensed fraction is supplied via line 337 as reflux to ultra high purity nitrogen column 104. No purge of any uncondensed fraction, if existent, is taken at this point. The return of the condensed fraction in line 337 to ultra high purity nitrogen column 104 is in contrast to the return of the condensed fraction from boiler/condenser 114 to first column 102 as described in Figure 1. Similarly to the process of Figure 1, a further refined nitrogen rich vapor stream having volatile light contaminants therein is withdrawn from an upper portion of first column 102 via line 314, partially condensed in boiler/condenser 108 with the condensed fraction being returned as reflux to first column 102 via line 316 and the uncondensed fraction removed via line 318. All other features of the process described in Figure 3 are similar to those in Figure 1. The basic operational difference between the embodiment of Figure 3 from that of Figure 1 is the reduction in a level of purge effected by this process. By taking purge only from boiler/condenser 108 the volume of purge may be substantially reduced from that process shown in Figure 1 and therefore there is less loss of nitrogen by virtue of this process. In addition the embodiment permits the withdrawal of product nitrogen via line 340 at a higher pressure from that of Figure 1. However, there may be a small penalty associated with the process in that ultra high purity nitrogen column 104 might require a few more trays to effect separation and concentration of the volatile light components in the overhead which is removed as an overhead via line 332. It is also worth noting that in Figure 3, both liquid nitrogen streams to the ultra high purity nitrogen column 104 may not be fed to the same location. For example, while liquid stream 337 may be fed at the top, liquid stream 320 should be fed a couple of trays below the top. The following examples are provided to illustrate the embodiments of the invention and are not intended to restrict the scope thereof. Example 1 Ultra High Purity Liquid Nitrogen An air separation process using the apparatus described in Figure 1 was simulated. In this figure, feed air stream 12 containing light contaminants is fed at the bottom of the first column. A gaseous nitrogen stream 14 is withdrawn from the top of first column 102 and is rich in volatile contaminants. A liquid nitrogen stream 20 is also withdrawn from about 2-5 trays below the nitrogen withdrawal point as feed and reflux to the ultra high purity nitrogen column 104. No major product streams are withdrawn from the top of the first column and the top 2-5 trays increase the concentration of the lights in the vapor phase. A non-condensible purge (stream 18) is taken from the boiler/condenser located at the top of the first column. This purge contains a fairly high concentration of the lights and is responsible for removing the majority of the light contaminants from the system. Alternatively, no purge need be taken and substantially all of the stream may be condensed and the volatiles allowed to concentrate for removal via line 41. These two streams are responsible for recovery in the process in the sense that the higher the flow rate the lower the recovery. However, because each stream is concentrated in lights. their volume may be maintained at a low level thereby enhancing recovery. Sample calculations for the flowsheet in Figure 1 were done for a preselected process design. The table sets forth the conditions: AIR SEPARATION FOR PRODUCING ULTRA HIGH PURITY NITROGEN PROCESS CONDITIONS FOR THE FIGURE Stream Component T °F(°C) P psia (kPa) F lb moles hr (kg moles hr) Impurity Concentration He H 2 Ne 12 air -269.9 (-167.7) 126 (869) 100 (45.4) 5.2 ppm 10 ppm 18.2 ppm 20 N 2 -277.6 (-172.0) 122 (841) 41.1 (18.6) 0.05 ppm 0.35 ppm 0.58 ppm 28 purge -279.9 (-173.3) 122 (841) 0.05 (0.02) 1.04% 1.97% 3.58% 32 N 2 -277.6 (-172.0) 122 (841) 2.9 (1.3) 0.66 ppm 4.96 ppm 8.32 ppm 34 N 2 -277.5 (-171.9) 122 (841) 38.2 (17.3) <0.01 ppb 0.05 ppb 0.05 ppb 35 N 2 -277.7 (-172.1) 122 (841) 37.7 (17.1) 89 ppm 0.06% 0.11% 40 N 2 -280 (-173.3) 110 (758) 38.2(17.3) <0.01 ppb 0.05 ppb 0.05 ppb The process described in the figure results in high nitrogen recovery of ultra high purity product via line 38 and line 40 with an extremely low impurity level. Note the level of total contaminants is 0.11 ppb impurities.

Claims: A process for producing an ultra high purity nitrogen product by the cryogenic separation, in an integrated multi-column distillation system comprising a first distillation column (102) and an ultra high purity nitrogen distillation column (104), of air comprising volatile impurities, wherein an air stream (10) is compressed, freed of condensible impurities, and cooled (100) generating a feed (12) for the integrated multi-column distillation system, said process comprising: a) generating a nitrogen rich vapour (14,35) containing volatile impurities in an upper part of the first column (102) and a crude liquid oxygen fraction (42) in a lower part of said first column (102); b) removing at least a fraction (14,35) of said nitrogen-rich vapour containing volatile impurities and partially condensing (108,114) at least a portion of said stream thereby forming a first condensed fraction (16,37) and an uncondensed fraction (18,41); c) returning at least a portion of said first condensed fraction (16,37) as reflux to the first column (102) in the distillation system; d) removing at least a portion of the uncondensed nitrogen rich vapour fraction rich (18,41) in volatile impurities generated in step b) as a purge stream; e) generating a liquid nitrogen fraction (20) in an upper part of said first column (102) and removing said liquid nitrogen fraction from the first column (102) at a location at or below that at which said nitrogen rich vapour is removed; f) introducing the liquid nitrogen fraction (20) to an upper part of the ultra high purity nitrogen column (104) as feed, said column (104) operating at the same pressure as the first column (102); g) generating a nitrogen rich vapour fraction (32) containing residual volatile impurities in the ultra high purity nitrogen column (104), removing that fraction as an overhead and returning the fraction to the first column; and h) removing an ultra high purity nitrogen fraction from the ultra high purity nitrogen column (104), wherein said ultra high purity nitrogen fraction (104) is expanded and warmed against a fraction of the nitrogen rich vapour (35) containing volatile impurities from the first column (102) in a boiler/condenser (114) thereby at least partially condensing a fraction (37) of the nitrogen rich vapour, separating the condensed fraction (37) from any uncondensed vapour fraction (41), and returning the condensed fraction (37) to the first distillation column (102) or the ultra high purity distillation column (104). A process as claimed in Claim 1, wherein a portion of said nitrogen rich vapour fraction (14) containing volatile impurities from the first column (102) is at least partially condensed against crude liquid oxygen (43) in a boiler/condenser (108) located at the top of the first column (102) to provide a condensed fraction (16) which is returned to the first column (102) as reflux. A process as claimed in Claim 2, wherein crude liquid oxygen (42) from the bottom of the first column (102) is charged to a boiler/condenser (110) in the bottom portion of the ultra high purity nitrogen column (104), cooled by indirect heat exchange, expanded and charged to the vaporizer side of the boiler/condenser (108) located at the top of the first column (102). A process as claimed in any one of the preceding claims, wherein an uncondensed vapour fraction (41) is removed from said boiler/condenser (114) as a purge stream. A process as claimed in Claim 4, wherein the condensed nitrogen rich vapour fraction (37) reduced in volatile impurities is returned to the first column (102) at an upper portion as reflux. A process as claimed in Claim 4 or Claim 5, wherein a liquid and vapour fraction (38,40) are generated on the vapour side of the boiler/condenser (114) and at least a portion of the nitrogen liquid (38) is recovered as ultra high purity product. A process as claimed in any one of Claims 4 to 6, wherein at least a portion of the nitrogen vapour (40) is recovered from the vapour side of the boiler/condenser (114) as ultra high purity product. A process as claimed in any one of Claims 4, 6 and 7, wherein the nitrogen rich vapour fraction (237) condensed in the boiler/condenser (114) is returned as reflux to the ultra high purity nitrogen column (104). A process as claimed in any one of the preceding claims, wherein the liquid nitrogen fraction (20) is removed from the first column (102) at a point below the removal point for the nitrogen rich vapour (14,35) containing volatile impurities. A process as claimed in any one of Claims 1 to 8, wherein the liquid nitrogen fraction (220) is removed from the first column (102) at substantially the same point as the removal point for the nitrogen rich vapour (214,235) containing volatile impurities. An integrated multi-column distillation system comprising a first distillation column (102) and an ultra high purity nitrogen distillation column (104) for producing an ultra high purity nitrogen product by the cryogenic separation of air comprising volatile impurities by the process of Claim 1, the system comprising: means (10,100,12) for producing a cold, compressed air feed free of condensible impurities and feeding same to the first column (102); condensing means (108,114) for partially condensing at least a portion of a fraction of nitrogen-rich vapour (14,35) containing volatile impurities removed from an upper part of the first column (102) to form a first condensed fraction and an uncondensed fraction; conduit means (16,37) for returning at least a portion of said first condensed fraction as reflux to the first column (102) in the distillation system; conduit means (18,41) for removing at least a portion of said uncondensed nitrogen as a purge stream; conduit means (20) for introducing as feed a liquid nitrogen fraction from an upper part of the first column (102) at a location at or below that at which said nitrogen rich vapour is removed to an upper part of the ultra high purity nitrogen column (104); conduit means (32) for removing as overhead a nitrogen rich vapour fraction containing residual volatile impurities from the ultra high purity nitrogen column and returning said fraction to the first column (102) at the same pressure; conduit means (34) for removing an ultra high purity nitrogen fraction from the ultra high purity nitrogen column (104); and a boiler/condenser (114) for expanding the liquid nitrogen removed by the conduit means (34) and warming it against a fraction of the nitrogen rich vapour (35) containing volatile impurities from the first column (102) thereby at least partially condensing a fraction of the nitrogen rich vapour. A system as claimed in Claim 11, further comprising means for separating said condensed fraction from the uncondensed vapour fraction (41) and removing any uncondensed vapour fraction as a purge stream. A system as claimed in Claim 12, further comprising conduit means (37) for returning said separated condensed nitrogen rich vapour fraction to the first column (102) at an upper portion as reflux. A system as claimed in Claim 12, further comprising conduit means (237) for returning said separated condensed nitrogen rich vapour fraction as reflux to the ultra high purity nitrogen column (104).

Inventors: AGRAWAL RAKESH, AGRAWAL, RAKESH
Applicants: AIR PROD & CHEM, AIR PRODUCTS AND CHEMICALS, INC.
Application year: 1992
Main classification: F25J3
IPC codes: F25J3, C01B21