Process and apparatus for producing pressurized gaseous nitrogen by cryogenic separation of air

Abstract

Process and apparatus for producing pressurized gaseous nitrogen by cryogenic separation of air. The distillation column system includes a high pressure column, a medium pressure column, a main condenser and top condenser both being condenser-evaporators. Compressed and purified feed air is cooled in a heat exchanger and introduced to the distillation system. A gaseous nitrogen stream from the high pressure column is condensed in the main condenser. Bottom liquid of the medium pressure column is evaporated and gaseous nitrogen from the medium pressure column is condensed in the top condenser. Liquid nitrogen from the medium pressure column is pressurized and introduced to the high pressure column. A second gaseous nitrogen stream from the high pressure column is recovered as pressurized gaseous nitrogen product. A portion of the compressed and purified feed air is work-expanded and then warmed in the main heat exchanger.

Claims

1. A process for producing pressurized gaseous nitrogen by cryogenic separation of air in a distillation column system comprising a high pressure column, a medium pressure column, a main condenser which is a condenser-evaporator having a liquefaction space and an evaporation space, and a medium pressure column top condenser which is a condenser-evaporator having liquefaction space and an evaporation space, compressing the total feed air in a main air compressor to a pressure which is higher than the operating pressure at the top of the high pressure column, purifying the compressed air stream, introducing the compressed and purified feed air stream into a main heat exchanger under a first pressure and cooling said compressed and purified feed air stream in said main heat exchanger, condensing a first gaseous nitrogen stream removed from the top of the high pressure column in a liquefaction space of the main condenser, removing bottom liquid from the high pressure column and introducing said bottom liquid of the high pressure column into an intermediate section of the medium pressure column, removing bottom liquid from the medium pressure column and introducing said bottom liquid of the medium pressure column into an evaporation space of the medium pressure column top condenser, removing gaseous nitrogen from the top of the medium pressure column and condensing the gaseous nitrogen in the liquefaction space of the medium pressure column top condenser, removing liquid nitrogen from the medium pressure column or from the liquefaction space of the medium pressure column top condenser and pressurizing the liquid nitrogen to a pressure which is at least equal to the high pressure column pressure to form pressurized liquid nitrogen, introducing at least a portion of the pressurized liquid nitrogen into the high pressure column, removing a second gaseous nitrogen stream from the top the high pressure column and warming the second gaseous nitrogen stream in the main heat exchanger, and recovering the warmed second gaseous nitrogen stream as the pressurized gaseous nitrogen product, and splitting the compressed and purified feed air stream into a turbine stream and a non-turbine stream, cooling the non-turbine stream in the main heat exchanger, introducing the non-turbine stream into the distillation column system, and work-expanding the turbine stream in an expansion machine, wherein the compressed and purified feed air stream is split at an intermediate temperature of the main heat exchanger into said turbine stream and said non-turbine stream, the turbine stream is work-expanded in the expansion machine from the first pressure to a second pressure to form a work-expanded turbine stream, and the work-expanded turbine stream is warmed in the main heat exchanger.

2. The process according to claim 1, wherein a waste stream taken from vapor produced in the evaporation space of the medium pressure column top condenser is warmed in the main heat exchanger and the work-expanded turbine stream is mixed with the waste stream upstream the main heat exchanger.

3. The process according to claim 1, wherein a cryogenic liquid from an external source is introduced into the distillation column system.

4. The process according to claim 3, wherein the cryogenic liquid is introduced into the distillation column system at one or more of the following places: the medium pressure column, the high pressure column, the pressurized liquid nitrogen line upstream or downstream of the pressurization of the liquid nitrogen, the evaporation space of the medium pressure column top condenser, and/or the evaporation space of the main condenser.

5. The process according to claim 1, wherein no gaseous nitrogen from the top of the medium pressure column is fed to the main heat exchanger and recovered as product.

6. The process according to claim 1, wherein all of the gaseous nitrogen produced at the top the medium pressure column is condensed in the liquefaction space of the medium pressure column top condenser.

7. The process according to claim 1, wherein the total feed air introduced into the distillation column system is obtained from the compressed and purified feed air stream that is introduced into the main heat exchanger under the first pressure.

8. The process according to claim 1, wherein the expansion machine used to expand the turbine stream is the single expansion machine used in the process.

9. The process according to claim 1, wherein the operating pressure at the top of the high pressure column is between 7.4 and 9.2 bars.

10. The process according to claim 1, wherein the second pressure that the turbine stream is expanded to is lower than 1.6 bar.

11. An apparatus for producing pressurized gaseous nitrogen by cryogenic separation of air comprising: a distillation column system comprising a high pressure column, a medium pressure column, a main condenser which is a condenser-evaporator having liquefaction space and an evaporation space, and a medium pressure column top condenser which is a condenser-evaporator having liquefaction space and an evaporation space, a main air compressor for compressing the total feed air to a first pressure which is higher than the operating pressure at the top of the high pressure column, a purification stage for purifying the compressed air stream, an air conduit for introducing the compressed and purified feed air stream into a main heat exchanger under a first pressure for cooling, a line for introducing at least a portion of the cooled air from the main heat exchanger into the distillation column system, a line for introducing a first gaseous nitrogen stream from the top the high pressure column into liquefaction space of the main condenser, a line for introducing bottom liquid from the high pressure column to an intermediate section of the medium pressure column, a line for introducing bottom liquid from the medium pressure column into the evaporation space of the medium pressure column top condenser, a line for introducing gaseous nitrogen from the top the medium pressure column into the liquefaction space of the medium pressure column top condenser, a pump for pressurizing liquid nitrogen from the medium pressure column or from the liquefaction space of the medium pressure column top condenser to a pressure which is at least equal to the high pressure column pressure, a line for introducing at least a portion of pressurized liquid nitrogen into the high pressure column, a line for introducing a second gaseous nitrogen stream from the top the high pressure column into the main heat exchanger, a line for recovering the second gaseous nitrogen stream, after warming in the main heat exchanger, as the pressurized gaseous nitrogen product, piping for splitting the compressed and purified feed air stream into a turbine stream and a non-turbine stream, means within the main heat exchanger for cooling the non-turbine stream and for a line for introducing the non-turbine stream from the main heat exchanger into the distillation column system, and an expansion machine for work-expanding the turbine stream, wherein the piping for splitting the compressed and purified feed air stream into a turbine stream and a non-turbine stream is located at an intermediate temperature of the main heat exchanger, wherein the expansion machine is formed and connected for work-expanding the turbine stream from the first pressure to a second pressure, and further comprising means within the main heat exchanger for warming the work-expanded turbine stream.

12. The apparatus according to claim 11, wherein said expansion machine is the single expansion machine.

13. The apparatus according to claim 11, wherein an outlet of the expansion machine is connected with a waste gas line coming from the evaporation space of the medium pressure column top condenser.

14. The process according to claim 1, wherein the operating pressure at the top of the high pressure column is between 7.6 and 8.5 bars.

15. The process according to claim 1, wherein the second pressure that the turbine stream is expanded to is in the range of 1.2 to 1.4 bar.

16. The process according to claim 1, wherein the operating pressure at the top of the medium pressure column is in the range of 3.7 bar to 4.6 bar.

17. The process according to claim 1, wherein the operating pressure at the top of the medium pressure column is in the range of 3.9 bar to 4.3 bar.

18. The process according to claim 1, wherein, after being cooled in the main heat exchanger, said non-turbine stream is introduced into said high pressure column of said distillation column system.

19. The process according to claim 1, wherein said expansion machine is a turbine.

20. The process according to claim 1, wherein a cryogenic liquid produced by the process is introduced into the distillation column system.

21. The process according to claim 20, wherein the cryogenic liquid is introduced into the distillation column system at one or more of the following places: the medium pressure column, the high pressure column, the pressurized liquid nitrogen line upstream or downstream of the pressurization of the liquid nitrogen, the evaporation space of the medium pressure column top condenser, and/or the evaporation space of the main condenser.

Description

(1) The invention is further described on the basis of an embodiment shown in the drawing.

(2) The total feed air 1 is compressed in a main air compressor 50 to a first pressure of e.g. 8.2 bars. The compressed air stream 51 is purified in a molecular sieve station 52, The compressed and purified air 53 is introduced at the first pressure to a main heat exchanger 2 at its warm end. A first portion of the air (non-turbine air) 3 is cooled to the cold end of the main heat exchanger 2 and introduced into a high pressure column 4. The high pressure column 4 is operated at a pressure of e.g. 7.9 bar at the top. It is a part of a distillation column system which further comprises a medium pressure column 5, a main condenser 6 and a medium pressure column top condenser 7. Both condensers 6, 7 are constructed as condenser-evaporators.

(3) A first gaseous nitrogen stream from the top the high pressure column is totally condensed in the liquefaction space of the main condenser 6. The liquid nitrogen 9 produced in the main condenser 6 is introduced into the top of the high pressure column 4 as reflux. Bottom liquid of the high pressure column (crude liquid oxygen) 10 is cooled in a first subcooler 11 and expanded to medium pressure column pressure in a valve 12. The expanded crude oxygen 13 is sent to an intermediate section of the medium pressure column 5.

(4) A first stream 14 of oxygen-enriched bottom liquid of the medium pressure column 5 is sent to the evaporation space of the main condenser 6 and at least partially evaporated. The evaporated first stream 15 is fed back to the medium pressure column bottom and serves as rising vapour inside the medium pressure column 5.

(5) A second stream 16 of oxygen-enriched bottom liquid of the medium pressure column 5 is cooled in a second subcooler 17 and in a third subcooler 18. Controlled by valve 20, the subcooled liquid 19, 21, 22, 23 is sent to the evaporation space of the medium pressure column top condenser 7. A small portion may be withdrawn as purge stream 24. Controlled by valve 27, the vapour 25, 26 from the evaporation space of the medium pressure column top condenser 7 is sent as waste gas to subcoolers 18, 11. The prewarmed waste gas 28 is fully warmed in the main heat exchanger 2. The warm waste gas 29 is vented and/or used in the molecular sieve station as regenerating gas.

(6) Gaseous nitrogen 30 from the top the medium pressure column 5 is condensed in the liquefaction space of the medium pressure column top condenser 7. Liquid nitrogen 31 produced thereby is fed back to a cup 32 in the top of the medium pressure column 4. A first portion of such liquid nitrogen is used as reflux in the medium pressure column 5. A second portion 53 of such liquid nitrogen is withdrawn from the medium pressure column 4, pressurized in a pump 33 to a pressure which is at least equal, preferably higher than the high pressure column pressure. At least a first portion 34, 36 of the pressurized liquid nitrogen flows through pump pressure control valve 35 and subcooler 17 into the high pressure column 4. If necessary, a second portion 37 of the pumped liquid nitrogen may flow through re-circulation path 38, 39 back to the medium pressure column 5.

(7) A second gaseous nitrogen stream 40 from the top the high pressure column 4 is warmed in the main heat exchanger 2. The warmed second gaseous nitrogen stream 41 is recovered as pressurized gaseous nitrogen product.

(8) In the embodiment, the primary source of refrigeration is an air turbine 42. The compressed and purified feed air stream 1 is split at an intermediate temperature of the main heat exchanger 2 into a turbine stream 43 and the non-turbine stream 3. The turbine stream is work-expanded in the air turbine 42 from the first pressure to a second pressure. The work-expanded turbine stream 44 is mixed with the waste stream 28 upstream the main heat exchanger 2. The mixed stream is warmed in main heat exchanger 2. The air turbine can be braked by any known brake mechanism, preferably by an oil brake, an air brake, oil bearing, gas bearing or foil bearing. Preferably no booster compressor is coupled to the air turbine.

(9) As additional source of refrigeration by liquid assist, a cryogenic liquid 45 from an external source, e.g., liquid nitrogen can be introduced into the medium pressure column 5 (as shown in the drawing) or into the high pressure column 4 (not shown). The plant as shown can be operated differently at different points of time: air turbine running, no liquid assist air turbine running combined with liquid assist air turbine not running-liquid assist only.

(10) In a particular embodiment of the invention, in a first operating mode, a portion of the pumped liquid nitrogen 34, 37 is recovered under pressure and stored in a pressurized liquid nitrogen tank (not shown in the drawing). In a second operating mode, the air turbine is shut off or operated with reduced throughput, and the stored liquid is taken for liquid assist (line 45).

(11) Coming back to the drawing, the dashed line around the large rectangle indicates the outer wall of a first cold box 46 surrounding all cryogenic parts except the nitrogen pump 33. The space between the apparatus and the outer wall is filled with pulverised insulation material like perlite. There is a separate cold box section 47 enclosing the nitrogen pump 33 only.

(12) In another plant, the air turbine is omitted and the plant is steadily run with liquid assist as the single source of refrigeration.

(13) In yet another plant, the nitrogen pump is omitted and a gaseous nitrogen stream from the top of the medium pressure column is warmed in the main heat exchanger and withdrawn as gaseous pressurized product. It can separately warmed from the high pressure column gaseous nitrogen product, so that two pressurized gaseous nitrogen products are recovered under different pressures, or the high pressure column gaseous nitrogen product is expanded to medium pressure column pressure and then mixed with the medium pressure column gaseous nitrogen product.

(14) In yet another plant, the turbine expansion 42 is replaced by another type of cold production like a cryocooler, piston or sterling etc.