Patent Application
20170211879
The invention regards a process for producing pressurized gaseous nitrogen by cryogenic separation of air. It further concerns an apparatus for producing pressurized gaseous nitrogen by cryogenic separation of air.
“Condenser-evaporator” means a heat exchanger, in which a first, condensing fluid stream is brought in indirect heat exchanger with a second, evaporating fluid stream. Each condenser-evaporator comprises a liquefaction space and an evaporation space which consist of liquefaction passages respectively evaporation passages. In the liquefaction space, the condensation (liquefaction) of the first fluid stream is performed; in the evaporation space the evaporation of the second fluid stream is conducted. Evaporation and liquefaction spaces are formed by groups of passages, which are in heat transfer relationship. The evaporation space of a condenser-evaporator can be realized as a bath evaporator, a falling film evaporator or a forced-flow evaporator.
The above kind of process and an apparatus are known from U.S. Pat. No. 6868207 [P16C012-EPR3, L'AL2003]. The refrigeration is provided either by liquid assist or by a turbine exhausting into the medium pressure column or by both. The first variant consumes cold and thereby energy from the outside, the second variant does not, but incorporates operational problems.
The problem solved by the invention is to minimise influences of the cold production on the distillation and thereby ensuring a particularly smooth and flexible operation of the system as a whole.
Such problem is solved by the features of the invention. By this special turbine configuration expanding a portion of the feed air from about high pressure column pressure to normally somewhat above atmospheric pressure, turbine expansion is completely decoupled from distillation, as no fluid from the distillation is sent to turbine. There is also no additional compressor needed to produce the cold.
The work-expanded air can be e.g. sent to the medium pressure column, in particular to its bottom, or by-passed around the distillation, e.g. by a separate main heat exchanger passage warming the work-expanded air to up to the warm end of the main heat exchanger and rejecting it to the atmosphere.
In a preferred embodiment of the invention, however, the work-expanded turbine stream is mixed with a waste stream upstream the main heat exchanger, such waste stream being taken from the vapour produced in the evaporation space of the medium pressure column top condenser. As a consequence, also no fluid to the distillation goes through the turbine, i.e. there is a full decoupling of refrigeration production and distillation. Simultaneously, the main heat exchanger configuration is nearly as simple and compact as in the liquid assist variant, as there is no separate group of passages needed for the work-expanded air; just an intermediate withdrawal for the turbine air must be provided.
A portion of the refrigeration requirements can be provided by liquid assist, i.e. by introducing a cryogenic liquid from an external source and/or by using a cryogenic liquid that has been internally produced at another point of time into the distillation column system. In the first alternative, the cryogenic liquid comes from another air separation or nitrogen liquefaction plant, or from a tank which filled by such other plant. In the second alternative, at least a portion of the cryogenic liquid is produced by the process itself, e.g. during periods of low energy cost and/or low product demand, and re-introduced to the plant during periods of higher energy cost and/or higher product demand. By this method, there can be, e.g. a constant production of gaseous nitrogen with varying energy consumption.
The cryogenic liquid is preferably liquid nitrogen, but any other mixture or pure fraction of liquefied air gases may be used as well. In principle, the plant may also be operated by liquid assist only, i.e. without a turbine.
The introduction of the liquid is performed at one or more of the following places:
Preferably, no gaseous nitrogen from the top of the medium pressure column is fed to the main heat exchanger and recovered as product. Even more preferably, the complete gaseous nitrogen produced at the top the medium pressure column is condensed in the liquefaction space of the medium pressure column top condenser and then pumped to at least high pressure column pressure and finally withdrawn as pressurized gaseous nitrogen under at least high pressure column pressure. Thereby, all the nitrogen produced is naturally recovered under the higher distillation pressure. The high pressure column gaseous nitrogen can of course be further compressed in one or more nitrogen compressors.
It is advantageous, if the compressed and purified feed air stream that is introduced into the main heat exchanger under the first pressure comprises the total feed air for the distillation column system. As a consequence, only a single group of passages for cooling air in the main heat exchanger and only a single air compressor is required.
Preferably, the expansion machine exanpding the turbine stream is the single expansion machine in the process. There is no other cold production in the system except, optionally, liquid assist, i.e introducing liquid produced at other places or at different times into the distillation system. This makes the respective plant compact and cheap.
The operating pressure at the top of the high pressure column is preferably chosen in the invention to be between 7.4 and 9.2 bars, in particular between 7.6 and 8.5 bars.
Preferably, the second pressure the turbine stream is expanded to, is lower than 1.6 bar, and lies in particular in the range of 1.2 to 1.4 bar.
In general, in the invention, the preferred ranges of the operating pressures of the columns at their tops are:
Moreover, the invention regards an apparatus for producing pressurized gaseous nitrogen. The apparatus according the invention may be supplemented by apparatus features described herein.
The invention is further described on the basis of an embodiment shown in the drawing.
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.
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.
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.
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.
Gaseous nitrogen 30 from the top the medium pressure column 4 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.
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.
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 of . . . bar. 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.
As additional source of refrigeration by “liquid assist”, a cryogenic liquid from an external source, e.g. liquid nitrogen 45 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:
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).
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.
In another plant, the air turbine is omitted and the plant is steadily run with liquid assist as the single source of refrigeration.
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.
In yet another plant, the turbine expansion 42 is replaced by another type of cold production like a cryocooler, piston or sterling etc.
| Number | Date | Country | Kind |
|---|---|---|---|
| 16000148.3 | Jan 2016 | EP | regional |
