IE65884B1 - Process and apparatus for producing nitrogen from air - Google Patents

Description

Process and Apparatus for Producing Nitrogen from Air The present invention is directed to a cryogenic superatmospheric process and apparatus for the separation of air to produce gaseous nitrogen and optionally liquid nitrogen.

Processes for the separation of air to produce nitrogen are knovn, as disclosed for example, in Ruhemann et al., U.S. Patent No. 3,203,193 and Keith, Jr., U.S. Patent No. 3,217,502. These processes provide for the operation of a single distillation column at a slightly higher pressure Ιθ than the product delivery pressure to separate a gaseous nitrogen product. Oxygen-enriched liquid air is vithdravn from the distillation column and is vaporised. Refrigeration is provided by further expanding the vaporised oxygen enriched air, also termed waste nitrogen. Such methods are able to recover up to about 35 to 40 mole percent of the feed air as nitrogen product.

Patel et al., U.S. Patent No. 4,400,188, discloses the use of a heat pump to separate nitrogen. The process, hovever, is only cost effective for the production of very large quantities of nitrogen, e.g. 15 to 200 million standard cubic feet/day (SCFD) (that is, 625,000 to 8,000,000 SCFH). To enhance separation the process uses overhead vapour recompression which requires complex and costly equipment making it uneconomical for recoveries in the range of less than about 15 million SCFD (625,000 SCFH). - 2 Conventional single distillation column systems, which expand waste nitrogen in a turboexpander for refrigeration generally filter and compress the feed air to above the nitrogen delivery pressure. The air is purified by removal of its carbon dioxide and water vapour content in beds of adsorbent, such as molecular sieve, and then cooled to near its dew point temperature. Alternatively, carbon dioxide and water vapour are removed in a reversing heat exchanger, in which the air and waste stream passages can be alternated, which allows the deposited impurities to evaporate into the waste stream which is ejected to the atmosphere.

The cooled air stream is fed to a distillation column where it is separated into an oxygen-rich liquid at the base of the column and a substantially pure nitrogen gas stream at the top. A portion of the pure nitrogen gas is warmed to ambient temperature and delivered as product. The balance is sent to a condenser to provide column reflux. Vaporised oxygen-rich liquid (sometimes termed waste nitrogen) from the condenser is warmed in a heat exchanger and then expanded in a turboexpander to provide refrigeration for the system.

Such systems characteristically recover only about 35-45 mole percent of the feed air as nitrogen product. It would therefore be an advace in the art if the mole percent recovery of nitrogen from the feed airaould be significantly increased.

According to the present invention, there is provided a process for the recovery of substantially pure nitrogen product at superatmospheric pressure from air comprising the steps of: (a) compressing gaseous feed air; (b) cooling the compressed air in a heat exchanger by heat exchange with enriched oxygen and nitrogen product streams; (c) introducing the cooled and compressed air to an intermediate stage of a single distillation column; (d) separating the air in the column into a substantially pure gaseous nitrogen overhead fraction and an oxygen-enriched liquid bottoms fraction and withdrawing a stream of each fraction from the column; -βίε) forwarding substantially all of the oxygen-enriched liquid bottoms stream and a portion of the gaseous nitrogen overhead stream to a condenser and therein indirectly exchanging heat between the bottoms stream and overhead stream thereby boiling oxygen-enriched liquid to form an oxygen-enriched gas stream and condensing liquid gaseous nitrogen to form a liquid nitrogen stream; (f) recycling at least a major portion of the resulting liquid nitrogen stream to the top of the distillation column as reflux; (g) introducing at least a first portion of the oxygen-enriched gas at a cryogenic temperature into a compressor, compressing said first portion of the oxygen-enriched gas stream, and recycling the compressed first portion of the oxygen-enriched gas stream to the bottom of the distillation column thereby enhancing nitrogen product recovery from the air; (h) warming the remainder of the gaseous nitrogen overhead stream in the heat exchanger by said heat exchange with the compressed air; and (i) recovering the wanned nitrogen overhead stream as a substantially pure nitrogen product from the heat exchanger.

The invention also provides an apparatus for the production of nitrogen product from air comprising: (a) a first compressor for increasing the pressure of gaseous feed air; (b) a heat exchanger for cooling the high pressure air with nitrogen and oxygen-enriched products of distilled feed air; — (c) a distillation column for separating the cooled air into a substantially pure gaseous nitrogen overhead fraction and an oxygen-enriched liquid bottoms fraction and having an outlet for the nitrogen communicating with the heat exchanger; (d) a condenser for at least partially condensing a stream of the gaseous nitrogen overhead to form a liquid nitrogen stream by indirect heat exchange with a stream of the oxygen-enriched liquid bottoms fraction to form an oxygen-enriched gas stream; (e) a first recycle means for returning a major portion of the liquid nitrogen stream from the condenser to the distillation column as reflux; / - 4 (f) a second compressor for increasing the pressure of at least part of the oxygen-enriched gas stream, the second compressor being positioned such that in use it receives oxygen-enriched gas at a cryogenic temperature; and (g) a second recycle means for returning increased pressure oxygen enriched gas stream to the bottom of the distillation column thereby enhancing nitrogen product recovery; wherein in use the nitrogen product is recovered from the said heat exchanger.

Pure nitrogen product is produced by the invention at considerably less power than conventional systems employing a single distillation column. Further, at least a portion of the work output of a turboexpander may drive the compressor for compressing the recycled waste nitrogen. Also, liquid nitrogen may be recovered as a product.

The compressed air stream that is cooled in a heat exchanger against the nitrogen product stream and oxygen-enriched gas stream which are wanned is optionally treated to remove impurities such as in a reversing heat exchanger. Alternatively, molecular sieve may be used to remove impurities prior to forwarding the air to a non-reversing heat exchanger.

In accordance with an alternative aspect of the invention,—the first portion of the ’waste nitrogen1 (oxygen-enriched gas) is sent to a cold compressor without first being warmed to ambient temperature. Also, a portion of the work output from the turboexpander may be supplied to the cold compressor. Alternatively, even higher outputs of nitrogen product can be achieved by using all of the work output from the turboexpander to operate the cold compressor. In this case, refrigeration is supplied to the system from an external source such as additional liquid nitrogen being provided to the distillation column. - 5 The method and apparatus according to the invention are nov described by vay of example vith reference to the accompanying dravings, in vhich: O FIGURE 1 is a schematic flov diagram of one embodiment of the invention using a plurality of heat exchangers including a reversing heat exchanger S vherein the entire vaste nitrogen stream is varmed, and a portion of the varmed product is compressed and returned to the distillation column; FIGURE 2 is a schematic flov diagram of another embodiment of the varm compression cycle using one less heat exchanger; FIGURE 3 is a schematic flov diagram of another embodiment of the varm compression cycle using molecular sieve for air purification; FIGURE 4 is a schematic flov diagram of another embodiment of the 15 invention using cold compression of the vaste nitrogen recycle flov vherein at least a portion of the vork output from the expander is used to operate the cold recycle compressor; and FIGURE 5 is a schematic flov diagram of another embodiment of the 20 invention using.cold compression of the vaste nitrogen recycle flov by means of the total available shaft vork from the turboexpander, vherein refrigeration is supplied by an external source.

Referring to F^ure 1 of the dravings, a nitrogen recovery system 2 according the the present invention provides for a stream of feed air 4 to be fed into a compressor 6. The resulting compressed air stream is forvarded to an aftercooler 7 for the purposes of cooling and condensing vater vapour. Thereafter, the condensate is removed in a separator 8 and an air stream nov indicated by the reference 10 exits the separator 8.

The air stream 10 passes through heat exchanger 12 vhere the air stream is cooled by heat exchange vith an oxygen-enriched gas stream 14 and nitrogen product stream 16. In the embodiment shovn in Figure 1, heat exchanger 12 is a reversing heat exchanger in vhich air passages are periodically svitched vith vaste nitrogen passages so that vater and carbon dioxide deposited in solid form from the air are evaporated after - 6 a switch of the passages into the waste nitrogen stream. Appropriate valves and conduits are provided to enable the air and waste nitrogen passages to be so switched.

The cooled air stream leaving the heat exchanger 12, and now shown by the reference 18, enters an (optional) gas phase absorber 20 which absorbs impurities such as any residual carbon dioxide and hydrocarbons therefrom. The resulting filtered air stream now indicated by the reference 22 proceeds to an (optional) heat exchanger 24 vhere the air is further cooled against the countercurrent flow of oxygen enriched gas stream 26 from a turbo-expander 28.

The resulting cooled air stream now indicated by reference 30 exiting heat exchanger 24, is near saturation and may be partly in its liquid state, this stream enters a distillation column 32 at an intermediate (liquid-vapour contact or mass transfer) stage. The cooled air stream 30 is separated by (fractional) distillation into a substantially pure gaseous nitrogen overhead (fraction), a stream 34 of vhich exits at the top of the column 32, and a liquid oxygen-enriched fraction, a stream 36 of vhich passes out of the bottom of the column 32. The liquid stream 36 is cooled by passage through an (optional) heat exchanger 38 against (e.g. countercurrently to) an oxygen enriched gas stream 40 and nitrogen product gas stream 42. The resulting cooled oxygen-rich liquid stream now indicated by reference 44 passes through valve 45, its pressure thereby being induced, and then via line 47 to condenser 46 vhere it boils vhile condensing a portion or sub-stream 48 of the gaseous nitrogen overhead stream 34 through indirect heat exchange. (The stream 34 of nitrogen is divided into tvo portions or sub-streams, one of vhich is the sub-stream 48 and the other of vhich is the stream 42 that is passed through the heat exchanger 38 countercurrently to the liquid oxygen stream 36, thereby being vanned. This other stream of nitrogen leaves the heat exchanger 38 (and is nov indicated by the reference 54) and is then vanned to ambient temperature by passage through the heat exchanger 12 and thereafter is passed via line 17 out of the system 2 for use as product nitrogen.) Ί The condensed liquid nitrogen exits condenser 46 as a stream 50 of liquid. The stream 50 is then split, and a portion or sub-stream 51 is optionally collected in a conventional storage facility 52. The major portion, however, of the condensed liquid nitrogen stream 50 returns via line 53 to the distillation column 32 vhere it serves as reflux.

A first portion or sub-stream 55 of the oxygen-enriched gas stream 54 exiting heat exchanger 38 is heated by passage through heat exchanger 12, vhere it serves to cool the feed air stream 10. The gas stream 55 leaves the heat exchanger 12 at a position intermediate the ends of the heat Ιθ exchanger 12 and flovs through a (pipe) line 56. A second portion or sub-stream 58 of the oxygen-enriched gas stream 54 by-passes heat exchanger 12, and combines vith the varmed gas flowing through line 56. The combined gas stream indicated by reference 60 enters a turboexpander 28 and expands to nearly atmospheric pressure producing refrigeration required to keep the system 2 cold. Some of the second portion or sub-stream 58 may by-pass the turboexpander 28 and be reunited vith the rest of this sub-stream immediately downstream of the outlet of the turboexpander 28. The expanded gas stream exiting the turboexpander 28 (nov indicated by the reference 26) is used to cool the incoming air, 2θ first by passage through heat exchanger 24. The oxygen-enriched gas stream, nov indicated by reference 16, leaves the heat exchanger 24 and provides further cooling for the air by passage through the heat exchanger 12. The oxygen-enriched gas stream exiting heat exchanger 12 is shown as st^am 15. _ A third portion or sub-stream 62 of the oxygen-enriched gas stream is warmed by passage through a heat exchanger 64, preferably to ambient temperature. A portion or sub-stream 66 of the stream 62 is withdrawn from the heat exchanger 24 at a temperature intermediate those of the cool and varm ends thereof and is united vith the gas stream 60 that enters the turboexpander 28. The remainder of the stream 62 continues its passage through the heat exchanger 64 and exits the varm end of the heat exchanger 64. The oxygen-enriched gas stream (now indicated by the reference 68) is compressed in compressor 70 to a pressure about equal to or slightly greater than the operating pressure of the distillation - 8 column 32. The resulting compressed gas stream, now indicated by reference 71, is cooled in an after cooler 72, further cooled to a lov temperature by being returned through heat exchanger 64 from its warm to its cold end, and recycled via a line 74 to the bottom of the distillation column 32 vhere it serves as boil up, thus increasing the nitrogen recovery possible from the feed air. The addition of the feed air stream 30 at an intermediate stage and recycled oxygen-enriched gas stream at the bottom of the column 32 permits the mass transfer stages betveen the inlets for these tvo streams to be used as a stripping section.

In the embodiment shovn in FIGURE 2, a single heat exchanger performs the functions of the heat exchangers 12 and 64 of Figure 1. The single heat exchanger is indicated by the reference 112 in Figure 2. In all other respects, the embodiment shovn in Figure 2 is the same as that shovn in Figure 1, but before purposes of clarity the flov of the oxygen-enriched gas stream leaving the condenser above the distillation column is nov described.

The oxygen-enriched stream (140) is varmed by passage through an optional heat exchanger 138. The varmed gas stream nov indicated by reference 154 is divided into three portions or sub-streams. A first portion or sub-stream 155 of the oxygen enriched gas stream 154 is varmed in passage through the heat exchanger 112. The varmed gas stream leaves the heat exchanger, at apposition betveen the ends thereof through a line 156. A second portion or sub-stream of the oxygen-enriched gas stream 158 by-passes the heat exchanger 112 and combines vith the first portion or sub-stream 155 in the line 160. The combined stream enters turboexpander 128 and is expanded to nearly atmospheric pressure to provide refrigeration, and exits the system via optional heat exchanger 124 and the main reversing heat exchanger 112.

A third portion or sub-stream 162 of the oxygen-enriched gas stream 154 passes completely through the heat exchanger 112 and, nov indicated by reference 168, flows into the compressor 170. The resulting compressed gas stream, nov indicated by reference 171, is then passed through an - 9 after cooler 172, back through heat exchanger 112, and then via line 174 to the bottom of distillation column 132.

In Figure 2, the stream of nitrogen product withdrawn from the heat exchanger 112 is indicated by the reference 117.

Referring to Figure 3 of the drawings, there is illustrated an embodiment of the invention generally similar to that shown in Figure 2, but in which purification of the feed air occurs outside of any heat exchanger and therefore no heat exchanger of the reversing kind is employed. A Ιθ compressed feed air stream is passed to a pre-purification unit 277 vhich typically contains beds of molecular sieves of zeolitic material which is able to be regenerated and vhich removes impurities such as carbon dioxide, some hydrocarbons and vater vapour. A purified air stream 210 passes through the heat exchanger 212, through optional heat exchanger 224, and into the bottom of distillation column 232 via line 230.

In addition, the embodiment shown in Figure 3 differs from that shovn in Figure 2 vith respect to the treatment of the waste oxygen-enriched gas stream (vaste nitrogen) passing through the heat exchanger 212. A portion or sub-stream 276 of the vaste nitrogen stream 215 is sent to the pre-purification unit 277 to serve as regeneration gas, vhich is normally heated before entering the pre-purification unit 277,- and exits line 278. In operation, a first group of the beds of unit 277 is used to adsorb impurities fron^the incoming air, while the remaining beds are regenerated. Once the first group becomes appropriately laden vith impurities, the flov of air is switched to the remaining beds, and the first group regenerated. Thus, continuous operation of the unit 277 is made possible.

The embodiments shovn in Figures 1 to 3 are all directed to compression of a warm oxygen-enriched gas stream. That is, the vaste nitrogen stream (vhich is enriched in oxygen) is warmed to essentially ambient temperature by passage through a heat exchanger before being compressed and recycled to the distillation column. These embodiments all improve nitrogen recovery over that possible vithout compression of a recycle / - 10 waste nitrogen stream. Additional embodiments of this invention employ cold compression of the waste nitrogen as a means of achieving improved recoveries in an efficient manner. Such embodiments use firstly excess refrigeration energy available in the turboexpanded stream of the waste gas and secondly the shaft work, economy that can be achieved vhen compressing a gas in cold state. Typically, in plants in vhich the distillation column operating pressure is at least 100 psig, there is enough energy available in the turboexpansion of the waste nitrogen to cover the normal refrigeration, needs of the plant and to compress a substantial amount of the vaste gas recycle stream in order to increase nitrogen recovery. Such a scheme minimises the amount of equipment vhich needs to be installed, for example, a compressor wheel can be driven off the turboexpander shaft, and heat exchange passes for warming the vaste gas recycle stream to ambient temperature prior to compression and then cooling the compressed stream to low temperature folloving compression are eliminated. Of course, any such process vhich uses expansion of vaste nitrogen to drive a compressor vill reduce the amount of vaste nitrogen available for turboexpansion. At some point, nitrogen recovery by compression of recycling oxygen-enriched gas is maximised vhile sufficient such gas remains available to cover both the refrigeration needs of the plant and to supply the energy for the cold compressor.

This equilibrium point depends upon the column operating pressure, the refrigeration needs of the plant, i.e. relating to its size and any liquid production requirements, the efficiencies of both the turboexpander gy»d the cold compressor. There are other factors, eg, frictional pressure drops, and choice of temperatures of the. fluids flowing into both the turboexpander and the cold compressor, which also have a bearing on the equilibrium point.

The shaft output of the turboexpander is used to accomplish tvo distinct on tasks: (1) driving a cold compressor of the vaste nitrogen vhich is recycled to the distillation column, thereby improving the nitrogen recovery from the air feed to the distillation column, and (2) removing energy (as heat) from the cold process equipment by delivering a portion of the shaft energy to a dissipative brake in the surroundings.

* The embodiment illustrated in Figure 4 of the drawings shows the recycle 5 of cold oxygen-enriched gas, i.e. oxygen-rich gas that is compressed in its cold state vithout being warmed to ambient temperature in a heat exchanger. More specifically, a compressed and purified feed air stream 310 is cooled by passage through a heat exchanger 312. A portion or subsidiary stream 314 of the cooled air stream 310 is passed through an optional heat exchanger 316 in vhich it is further cooled and condensed before passing via line 318 into an intermediate stage of a distillation column 332. A second portion or subsidiary stream 320 of the cooled air stream 310 is passed directly to another, but lover, intermediate stage of the distillation column 332.

Air entering distillation column 332 is separated into a substantially pure gaseous nitrogen overhead exiting from the top of column 332 as stream 334 and an oxygen-enriched liquid bottom stream 336 exiting from the bottom of the column 332. The liquid stream 336 is cooled by passage 2θ through a heat exchanger 338 against a return oxygen-enriched gas stream 340 and a subsidiary or product stream 342 of nitrogen gas vhich is taken from the stream 334. The resulting cooled oxygen-enriched liquid stream, nov indicated by reference 344, is reduced in pressure by passage through valve 345, and enters condenser 346 via line 347. The oxygen-enriched 2-6- liquid stream boils in the condenser 346 vhile condensing a portion or sub-stream 348 of the gaseous nitrogen product stream 334 through indirect heat exchange. The condensed nitrogen is returned to the distillation column 332 to serve as reflux.

Resulting boiled oxygen-enriched gas is withdrawn as a stream 340 from the condenser 346 and is optionally warmed by passage through the heat exchanger 338. The stream of varmed oxygen-enriched gas leaving the heat exchanger 338, now indicated by the reference 301, is divided into three portions or sub-streams. One portion 302 of the oxygen-enriched gas stream 301 is not further varmed by heat exchange but enters a compressor z - 12 370 in which it is compressed. The resulting compressed gas stream, nov indicated by reference 303, is then returned via line 304 to the bottom of distillation column 332 after being cooled by passage through heat exchanger 312 from a first intermediate region thereof at a relatively high temperature to a second intermediate region thereof at a relatively lov temperature. A second portion or sub-stream 305 of the gas stream 301 is passed to the turboexpander 328 after passing through the heat exchanger 312 from its cold end to an intermediate region thereof. A third portion or sub-stream may by-pass the heat exchanger 312 via valve 306. The expanded gas stream leaving the turboexpander 328 passes through the heat exchanger 316 from its cold end to its varm end thereby providing cooling for the air stream 314, and then through the heat exchanger 312 from its cold end to its varm end thereby providing cooling for the incoming air stream 310. The stream 342 after passage through the heat exchanger 338 also passes through the heat exchanger 338 also passes through the heat exchanger 312 from its cold end to its varm end thereby exchanging heat for the air stream 310. The resulting varmed nitrogen stream nov indicated by reference 317 is taken as nitrogen product.

Of particular importance to this embodiment is that a shaft connection 307 is provided betveen the turboexpander 328 and the compressor 370. A portion of. the vork output of the turboexpander 328 is thus used to drive the compressor 370 thereby providing boil up” flov distillation column 332 .vhich enhances the recovery of the nitrogen product stream 317. Part of the vork output is directed to a dissipative brake 308 to remover heat from the system and reject this heat to the surroundings. Surroundings” means outside the cold box (not shovn) boundaries of energy and flov.

The dissipative brake 308 may be a compressor, a pump, electrical generator, or like device, or even friction in the bearings of a rotating part. It is important that the system directs requisite energy to the surroundings to keep the cold compression process refrigerated.

Vhereas the process shovn in Figure 4 requires some of the turboexpander shaft output to supply a dissipative brake to refrigerate the plant, the process shovn in Figure 5 of the dravings needs no dissipative brake I - 13 because some of its refrigeration is provided from an outside source.

The entire shaft output of the turbocompressor can be applied to driving a compressor; thus even higher recoveries of nitrogen from the air fed to A the distillation column are achievable. In all other respects, the embodiment of the invention illustrated in Figure 5 is the same as that illustrated in Figure 4. In such use of cold compression, shown in Figure 5, all of the available work output of the turboexpander 428 is supplied to a compressor 470. This enables a higher recovery of nitrogen product 417 to be obtained because an even greater boil up flov is achievable in column 432. In this event, refrigeration needs to be supplied to the system, for example, by supplying liquid nitrogen to the distillation column 432 from an external source 471, and there is no intentional dissipative brake.

If the external source 471 of refrigeration for the process of Figure 5 is liquid nitrogen at or near the purity of the desired gaseous product of the plant, a proportional increase in gaseous nitrogen product the plant can result. The amount of refrigeration from an external source is a function of the heat leak and enthalpies associated vith the fluid flows at the cold box boundaries.

The cold waste nitrogen compression is achieved by coupling the compressor 470 to the turboexpander 428 output exclusively, vhich is made possible by providing an external source of refrigeration. Such a scheme gains commercial attractiveness as the cost of supplying refrigerating substances 471 (e.g. liquid nitrogen) has diminished as producing plants for these liquids has become larger and more efficient.

The increase in nitrogen recovery made possible by dedicating the total output of the turboexpander 428 to recycle waste nitrogen compression further increases the amount of nitrogen gas per unit of liquid refrigerant 471 supplied, and therefore the economic return of the plant.

Another advantage of the process shown in Figure 5 is that only tvo cold machines are required, preferably connected by a common shaft. The additional mechanical complication of the dissipative device of FIGURE 4 is eliminated.

In the plants shovn in Figures 4 and 5, pre-purification of feed air is a preferred alternative to a reversing heat exchanger.

In another example of the use of cold compression (not. shovn), the energy for such compression comes from an external source, e.g., an electric motor. The electric motor is an external requirement and increases the refrigeration needs of the plant. Hovever, these are also met by the turboexpander vhich is free of the necessity of supplying shaft energy to Ιθ the cold compressor. Once again, hovever, as cold compression increases the recovery of nitrogen, the amount of waste nitrogen available for turboexpansion is reduced. Vhen this is reduced to the quantity required to meet the refrigeration needs of the plant (including that from the external energy source driving the cold compressor), then the maximum recovery of nitrogen has been reached.

EXAMPLE 1 A process for the recovery of substantially pure nitrogen at the rate of 110,000 standard cubic feet per hour (SCFH) at 114.7 psia is conducted in accordance vith FIGURE 1. SCFH refers to a substance measured as a gas at 14.7 psia and 70*F.

A feed air. flowof 185,169 SCFH vas compressed to a pressure of 125.3 psia, aftercooled to a temperature of 100°F, and then cooled in the heat exchanger 12. The cooled air stream vas passed via the line 18 at the rate of 183,336 SCFH and a temperature of -265.8®F to the gas phase absorber 20 for the removal of impurities. The air stream vas then cooled by passage through the heat exchanger 24. The cooled air having a liquid content of 0.03 mole percent (at -269.6°F and 122.2 psia) vas sent to an elevated tray (i.e. intermediate stage) of the distillation column 32.

Gaseous nitrogen at a pressure of 119.1 psia and a temperature of -278.4°F exited from the top of the distillation column 32 and a portion was forwarded to the heat exchanger 38 where the nitrogen was warmed to -268.5°F. A flow of 109,980 SCFH was warmed in heat exchanger 12. The final product was cooled at a temperature of 94.6°F and 118 psia to give a nitrogen recovery of about 59 mole percent based on total air compressed.

The oxygen enriched gas from condenser 46 passed through the heat exchanger 38 at the rate of 142,036 SCFH. A portion of this flow, 68,700 SCFH, passed completely through the heat exchanger 64 and was varmed to ambient temperature therein. The varmed gas vas then compressed to 123.3 psia and aftercooled to 100°F. The cooled gas re-entered the heat exchanger 64 and vas cooled to -257.3°F at a pressure of 122.5 psia for delivery to the bottom of the distillation column 32.

The balance of the oxygen enriched gas leaving the heat exchanger 38 vas divided betveen the heat exchangers 64 and 12 and by-pass line 58 to provide the feed gas to the turboexpander 28 and its by-pass, a total of 73,336 SCFH, at a pressure of 51.4 psia and temperature of -235°F. A flow of 60,790 SCFH of this gas 60 passed through the turboexpander 28 providing requisite refrigeration. The turboexpander exhaust gas and the by-pass was combined into line 26 and varmed in the heat exchangers 24 and 12.

EXAMPLE 2 * a flow of 25,000 SCFH of nitrogen vas produced in accordance vith the process described in FIGURE 4 vherein a portion of the work output from the turboexpander 328 vas sent to the compressor 370 via the shaft 307 and the balance vas transmitted out of the system.

An air flow of 51,546 SCFH vas fed at a pressure of 133 psia through the heat exchanger 312. Then 1036 SCFH of the cooled air vas sent through the heat exchanger 316 for condensing prior to delivery to an intermediate stage of the distillation column 332. The balance of the cooled air entered an elevated tray, belov the entry stage of line 318, of the distillation column 332 directly. The products of the - 16 distillation column 332 vere 65,758 SCFH nitrogen gas, of vhich 40,758 SCFH vas returned as reflux after condensing in condenser 346, and 36,211 SCFH of oxygen rich liquid stream 336. The oxygen rich liquid stream 336 was subcooled in the heat exchanger 338 and throttled through valve to about 68 psia for boiling in the condenser 346. Both the boiled oxygen rich gas stream 340 and 25,000 SCFH of the nitrogen (product) stream 342 were warmed in heat exchanger 338. The warmed nitrogen product stream entered the main heat exchanger 312, vas warmed to ambient temperature, and exited the system as stream 317.

The oxygen-enriched gas stream vas divided into a portion or sub-stream for turboexpansion and a portion or sub-stream for cold compression and recycle to or sub-stream distillation column, the relative flow rates being 26,546 SCFH and 9665 SCFH, respectively. The recycle gas vas compressed to 130 psia, cooled in heat exchanger 312 and injected into the bottom of the distillation column 332 for boil up. The gas stream passed to the turboexpander 328 vas first heated partially in heat exchanger 312 and expanded to about 18 psia in the turboexpander 328. It then passed through heat exchangers 316 and 312, yielding its refrigeration and becoming the vaste nitrogen product of the plant.

By these means, a nitrogen recovery of about 48.5 mole percent of the feed air vas attained. Various recoveries are achievable by this process, depending on the plant size, cold compressor and turboexpander efficiencies, t^e operating pressure of the distillation column, the number of trays in the distillation column, and the desired nitrogen __ purity.

In this Example, part of the shaft vork generated by the turboexpander 328 is transmitted to the surroundings and part to the cold compressor 303. Vork transmitted to the surroundings by brake 308 constitutes the refrigeration necessary to refrigerate the plant.

EXAMPLE 3 The same procedure vas follows as in Example 2 except that all of the / available work output from the turboexpander 428 was used to operate the compressor 470 in order to maximise recovery of nitrogen as illustrated in Figure 5. The cold box being well insulated, 949 SCFH of liquid nitrogen vas added to the top of the distillation column 432 to provide refrigeration. A feed air stream of 51,546 SCFH vas processed in the ’5 system to produce up to 30,000 SCFH of product nitrogen 417 resulting in a nitrogen recovery rate of about 58 mole percent of the feed air.

The present invention recovers substantially pure nitrogen product, both gas and liquid as desired, on the order of up to 70 mole percent. As plant size decreases, especially belov 800,000 SCFH, the present invention becomes more cost effective due to the absence of the standard column reboiler and the less expensive heat pump circuit comprising compression equipment.

A single turboexpander is not essential to this embodiment of the invention. If fact, one turboexpander serving the refrigeration needs of the plant and another driving the compressor for recycle to the column in order to provide higher nitrogen recovery is vithin the scope of the present invention. There are other combinations, in all of vhich the cold compression step uses shaft energy inherently produced in the process.

While particular embodiments of the invention have been described, it will, be understood, of course, that the invention is not limited thereto since many obvious modifications can be made, and it is intended to include vithin this invention any such modifications as vill fall vithin the scope of the invention as defined by the appended claims.

Claims (16)

Claims

1. A process for the recovery of substantially pure nitrogen product at superatmospheric pressure from air comprising the steps of: (a) compressing gaseous feed air; (b) cooling the compressed air in a heat exchanger by heat exchange with enriched oxygen and nitrogen product streams; (c) introducing the cooled and compressed air to an intermediate stage of a single distillation column; (d) separating the air in the column into a substantially pure gaseous nitrogen overhead fraction and an oxygen-enriched liquid bottoms fraction and withdrawing a stream of each fraction from the column; (e) forwarding substantially all of the oxygen-enriched liquid bottoms stream and a portion of the gaseous nitrogen overhead stream to a condenser and therein indirectly exchanging heat between the bottoms stream and overhead stream thereby boiling oxygen-enriched liquid to form an oxygen-enriched gas stream and condensing gaseous nitrogen to form a liquid nitrogen stream; (f) recycling at least a major portion of the resulting liquid nitrogen stream to the top of the distillation column as reflux; (g) introducing at least a first portion of the oxygen-enriched gas at a cryogenic temperature into a compressor, compressing said first portion of the oxygen-enriched gas stream, and recycling the compressed first portion of the oxygen-enriched gas stream to the bottom of the distillation column thereby enhancing nitrogen product recovery from the air; (h) warming the remainder of the gaseous nitrogen overhead stream in the heat exchanger by said heat exchange with the compressed air; and (i) recovering the wanned nitrogen overhead stream as a substantially pure nitrogen product from the heat exchanger.

2. A process according to Claim 1 further comprising expanding a second portion of the said oxygen-enriched gas stream in an expanding means thereby generating work output to provide refrigeration for the process. - 19

3. A process according to Claim 2, further comprising warming a third portion of the oxygen-enriched gas stream in the heat exchanger by heat exchange with the compressed air upstream of combination with said 5 second portion and expansion of the combination.

4. A process according to Claim 2 or Claim 3, wherein only part of the second portion is expanded while the remainder of the second portion by-passes the expanding means.

5. A process according to any one of the preceding claims, wherein the first portion of the oxygen-enriched gas stream of step (g) starts its compression at about a temperature of the distillation column. 15

6. A process according to Claim 5, further comprising utilising a portion of the work output obtained from the expanding means to compress the first portion of the oxygen-enriched gas stream which is recycled to the bottom of the distillation column. 20

7. A process according to Claim 5 or Claim 6, further comprising removing from the process a portion of the work output from the expansion means.

8. A process according to Claim 7, wherein the removed portion of the 25- work output is transferred to the surroundings as heat or work.

9. A process according to Claim 5, wherein all the work output is utilised to compress the first portion of the oxygen-enriched gas stream which is recycled to the bottom of the distillation column, and 30 further comprising adding refrigeration to the process from an external source.

10. A process according to Claim 9, wherein the step of adding refrigeration to the process comprises adding liquid nitrogen to the 35 distillation column.

11. Apparatus for the production of nitrogen product from air comprising: - 20 (a) a first compressor for increasing the pressure of gaseous feed air; (b) a heat exchanger for cooling the high pressure air with nitrogen and oxygen-enriched products of distilled feed air; (c) a distillation column for separating the cooled air into a substantially pure gaseous nitrogen overhead fraction and an oxygen-enriched liquid bottoms fraction and having an outlet for the nitrogen communicating with the heat exchanger; (d) a condenser for at least partially condensing a stream of the gaseous nitrogen overhead to form a liquid nitrogen stream by indirect heat exchange with a stream of the oxygen-enriched liquid bottoms fraction to form an oxygen-enriched gas stream; (e) a first recycle means for returning a major portion of the liquid nitrogen stream from the condenser to the distillation column as reflux; (f) a second compressor for increasing the pressure of at least part of the oxygen-enriched gas stream, the second compressor being positioned such that in use it receives oxygen-enriched gas at a cryogenic temperature; and (g) a second recycle means for returning increased pressure oxygen enriched gas stream to the bottom of the distillation column thereby enhancing nitrogen product recovery; wherein in use the nitrogen product is recovered from the said heat exchanger.

12. Apparatus according to Claim 11, in which the second compressor is coupled to a turboexpander for generating refrigeration.

13. Apparatus according to Claim 12, in which the second compressor is coupled to the turboexpander through a dissipative brake.

14. Apparatus according to any one of Claims 11 to 13, in which the second compressor is upstream of the cold end of the heat exchanger and downstream of the outlet of the condenser for the oxygen-rich gas stream. - 21

15. A process as defined in Claim 1 for the recovery of substantially pure nitrogen product at superatmospheric pressure from air, substantially as hereinbefore described by way of example and/or with reference to the accompanying drawings.

16. Apparatus as defined in Claim 11 for the production of nitrogen product, substantially as herein described by way of Example and/or with reference to the accompanying drawings.