Patent Application
20150316317
The invention relates to a method according to the preamble of Claim 1.
Methods and devices for the low-temperature separation of air are known, for example, from Hausen/Linde, Low-temperature technology, 2nd edition 1985, Chapter 4 (pages 281 to 337).
The distillation column system of the invention includes a two-column system (for example a classic Linde double column system) for nitrogen-oxygen separation having a high-pressure column and a low-pressure column, which are operatively interconnected for heat exchange. The operative interconnection for heat exchange between the high-pressure column and the low-pressure column, as a rule, is realized by a main condenser in which head gas of the high-pressure column is liquefied against evaporating sump liquid of the low-pressure column. In addition to the columns for nitrogen-oxygen separation, the distillation column system can comprise further devices, for example for producing other air components, in particular inert gases, for example producing argon which includes at least one raw argon column, or producing krypton-xenon. Along with the distillation columns, the distillation column system also includes the heat exchangers which are assigned directly to them and, as a rule, are realized as condenser-evaporators.
A “main heat exchanger”, in this case, serves for cooling the feed air in indirect heat exchange with return streams from the distillation column system. It can be formed by one single or several heat exchanger portions which are connected in parallel and/or in series, for example by one or several plate heat exchanger blocks.
In a secondary condenser, which is also realized as a condenser-evaporator, oxygen removed in the liquid state from the low-pressure column is evaporated at an only slightly increased oxygen pressure of between 1.5 and 6 bar, preferably between 2.7 and 4 bar. Part of the cooled feed air is liquefied against the evaporating oxygen.
A heat exchanger, in which a first condensing liquid stream enters into indirect heat exchange with a second evaporating liquid stream, is designated as a “condenses evaporator”. Each condenser-evaporator comprises a liquefaction chamber and an evaporation chamber which consist of liquefaction passages or evaporation passages. The condensing (liquefying) of a first liquid stream is carried out in the liquefaction chamber and the evaporation of a second liquid stream is carried out in the evaporation chamber. The evaporation chamber and the liquefaction chamber are formed by groups of passages which are operatively interconnected for heat exchange.
A method of the type mentioned in the introduction and a corresponding device are known from EP 1319913 A1 (=US 2003110796 A1). Pressurized nitrogen is also produced in this case from the distillation column system; however, this is only possible to a limited extent because there the respective flow is missing as reflux in the columns.
Within the framework of the invention, a method is sought that is capable of generating large volumes of nitrogen along with the oxygen at the slightly increased oxygen pressure and at the same time of keeping the number of externally driven machines, in particular of the compressors, which are not driven by a turbine of the method as small as possible. The oxygen, in this case, is to be generated either as pure oxygen with a purity of in excess of 99.5 mol-% or as non-pure oxygen with less purity, in particular with a purity of less than 98 mol-%. Along with a method of operation which is particularly favorable as far as energy is concerned, an arrangement that is as compact as possible is also to be obtained.
Said object is achieved by the features of Claim 1. A precolumn, which is known per se from WO 2009 095188 A2, is utilized in this case. The method of WO 2009 095188 A2 WO 2009 095188 A2, however, is chiefly directed toward the production of large volumes of oxygen under a very high pressure of clearly in excess of 6 bar as a result of internal compression. Pressurized nitrogen is certainly produced directly from the distillation column system in this case too, but this is only possible to a similarly small extent as in the case of the known secondary condenser method. The expert will therefore not at first expect to find a solution to the above-described technical problem in WO 2009 095188 A2.
Only within the framework of the invention has it been shown surprisingly that a method with a precolumn is not only suitable for internal compression, but also in conjunction with a secondary condenser, in which oxygen removed in the liquid state from the low-pressure column is evaporated at an only slightly increased oxygen pressure, results in removal of a large volume of pressurized nitrogen with a much higher yield. Over and above this, the method according to the invention, in contrast to the process of WO 2009 095188 A2, is preferably operated with a comparatively small amount of pre-liquefaction of the air; the liquid part of the feed air which is to be introduced into the distillation column system includes a maximum of 29 mol-% and is in particular between 23 and 29 mol-%.
The secondary condenser, the head condenser and the precolumn are arranged one above the other. An arrangement of two elements “one above another” is to be understood here as the upper end of the lower of the two elements being situated at a lower geodetic height than the lower end of the upper of the two elements and the projections of the two elements into a horizontal plane intersecting. For example, the two elements can be arranged precisely one above another, this means the axes of the two elements extend along the same vertical straight line.
In the case of the invention, three elements are arranged one above the other in the above-described sense such that overall a particularly compact method of construction is produced.
The operating pressure of the precolumn is preferably chosen such that it corresponds to the pressure of the second part stream of the air which is required for the oxygen evaporation in the secondary condenser. In particular, the operating pressure of the precolumn in the sump is preferably between 7.5 bar and 10.5 bar.
The first gaseous nitrogen product can be removed under precolumn pressure (at the head of said column). Said pressure, in this case, is approximately 9 bar. Depending on the desired end pressure, this means that a product compressor can be completely dispensed with or it can be realized with fewer stages than if the nitrogen product is removed from the low-pressure column or the high-pressure column. Within the framework of the invention, for example up to 30 mol-%, preferably between 5 and 25 mol-% of the feed air volume can be removed from the precolumn as a first gaseous nitrogen product.
In the case of the invention, preferably all of the feed air is compressed to the pressure of the precolumn (plus line losses) in the main air compressor (MAC). Consequently, there is no need for a booster air compressor (BAC) that is driven by way of external energy. In addition, savings are produced in the investment costs as a result of correspondingly smaller component parts in the “hot” part of the air separation unit (precooling and purification device) and there is a comparatively smaller amount spent on regeneration in the purification device.
The invention relates above all (but not only) to the area of relatively small units with extensive packaged units where dispensing with additional compressors plays a key role both in the time and money spent on equipment and maintenance and on energy consumption. Thus, for example, it is possible to dispense with small nitrogen booster compressors which regularly have a relatively poor efficiency level.
Because in the case of the invention only a relatively small portion of nitrogen is removed as a low-pressure nitrogen stream, the main heat exchanger has a correspondingly small volume and consequently there is a further reduction in the time and money spent on equipment.
In a first variant of the invention, the secondary condenser is arranged above the precolumn and in a second variant it is arranged below the precolumn.
In the case of the first variant, the secondary condenser and the head condenser can be arranged in a common container. For example, the container is realized as a vertical cylinder and comprises a tight horizontal intermediate floor between the two apparatuses.
In addition, according to claim 2, a second gaseous nitrogen product can be produced directly from the high-pressure column under, for example, between 5 and 6.5 bar, also without the use of a product compressor (and without low-pressure stages). This is particularly favorable when the customer requires nitrogen under different pressures which correspond approximately to the operating pressures of the precolumn and high-pressure column. In addition, both nitrogen products can be produced with different purities. In total (first and second gaseous nitrogen product) up to 50 mol-%, preferably between 25 and 50 mol-% of the feed air volume can be produced as a pressurized nitrogen product.
In the case of the invention, it is advantageous when cold is generated, according to claim 3, by a Claude turbine which is operated with a third part stream of feed air and expands into the high-pressure column. Said third part stream is not fully cooled in the main heat exchanger (that is not guided up to the cold end), but only up to an intermediate temperature. The corresponding expansion machine is preferably formed by an expansion turbine. Said expansion turbine can be coupled to a booster in which, in particular, the turbine stream (third part stream) is boosted upstream of the expansion for carrying out work.
In contrast to WO 2009 095188 A2, in the case of the method according to the invention a smaller oxygen concentration in the raw oxygen fraction is preferably produced in the sump of the precolumn than in the sump of the high-pressure column. The two raw oxygen fractions are consequently not mixed with one another, but, according to claim 4, are fed separately into the low-pressure column at different intermediate points. Between the two feed points there are, for example, between 5 and 20, preferably between 7 and 15 theoretical floors.
The invention also relates to a device for the low-temperature separation of air according to claims 8 to 13.
The following variants are possible within the framework of the invention and, where applicable, can also be combined together:
The invention and further details of the invention are explained in more detail below by way of three exemplary embodiments which are shown schematically in the drawing, in which:
In
The compressed and purified feed air 206 is cooled to a first part 210 in a main heat exchanger 260 up to the cold end thereof. The “first part stream” 1 and the “second part stream” 2a are formed from this. A “third part stream” 230 is recompressed in a booster compressor 466 with an aftercooler 467, guided via line 231 also to the hot end of the main heat exchanger 260, only cooled there however to an intermediate temperature and removed again. The cooled third part flow 232 is expanded in an expansion turbine 465 so as to carry out work and forwarded via line 233. The expansion turbine 465 and the booster compressor 466 are coupled in a mechanical manner.
In the case of the exemplary embodiment, the distillation column system includes a precolumn 10, a pressure column 11 and a low-pressure column 12 as well as the condenser-evaporator linked thereto, the main condenser 13 and the head condenser 14 of the precolumn. The secondary condenser 46 is not part of the distillation column system. As an option, the distillation column system can also comprise an argon part which includes, in particular, at least one raw argon column and its head condenser; in addition, the argon part can comprise a pure argon column for separating argon and nitrogen.
In the example, the separating columns for the separation of nitrogen and oxygen comprise the following operating pressures (in each case at the head):
The cooled gaseous (or somewhat pre-liquefied) first part stream 1 of the feed air from the cold end of the main heat exchanger 260 is under a pressure which is just above the operating pressure of the precolumn 10 and is introduced directly into the precolumn above the sump.
The precolumn 10 comprises a head condenser 14, into the liquefaction chamber of which a nitrogen stream 31 is introduced. A liquid second part stream 2b of the feed air (see below) is introduced into the evaporation chamber of the head condenser 14 of the precolumn 10. The rest of the feed air is introduced into the distillation column system, in particular into the high-pressure column, via the line 233 in the gaseous state or substantially gaseous state. A gaseous stream 16 which is enriched in oxygen is removed from the evaporation chamber of the head condenser 14 and mixed with the gaseous air 233. As an alternative to this, the streams 233 and 16 can be introduced separately (where applicable at different points) into the high-pressure column 11.
In the example, an additional liquid stream 4 is also directed into the evaporation chamber of the head condenser 14. This is formed by part of the sump liquid of the precolumn 10.
The remainder 5a, 5b of the sump liquid of the precolumn is undercooled here in an undercooling heat exchanger 37 and introduced into the low-pressure column 12, at an intermediate point above the feeding-in of the high-pressure column sump liquid 38. The liquid 6, which is generated from part 31 of the head nitrogen 30 of the precolumn 10 in the condensation chamber of the head condenser 14, is fed as head reflux into the precolumn 10. Part 8 of the reflux liquid can be removed a little further down (as shown) and guided to the head of the high-pressure column 11.
The evaporated fraction 16 formed in the evaporation chamber of the head condenser 14 is guided via line 17 to the sump of the high-pressure column 11, together with the third part stream 233 of the feed air which originates from the outlet of the Claude turbine 465. The flushing liquid 32a, 32b from the head condenser 14 of the precolumn 10 is supplied to the high-pressure column 11 at an intermediate point in the lower region.
Apart from this, the double column 11/12/13 functions in the generally known manner. From the high-pressure column 11, liquid raw oxygen 33 at the sump and liquid non-pure nitrogen 35 from an intermediate point relatively high up are cooled in an undercooling heat exchanger 37 in indirect heat exchange with return streams and are introduced into the low-pressure column 12 via the lines 38 or 40 at the suitable points.
The following products can be removed from the columns:
The gaseous product streams are healed with feed air in the main heat exchange 260 indirect heat exchange. The main heat exchanger can consist of one block or of two or several blocks which are connected in parallel and/or in series. The oxygen 50a removed in liquid form from the low-pressure column is pressurized in liquid form in a pump 55 to a pressure of, for example, between 2 and 5 bar, preferably between 2.7 and 4.0 bar, and is then directed via line 50b into the evaporation chamber of the secondary condenser 46. The evaporated oxygen 50c is heated in the main heat exchanger to approximately ambient temperature and is finally (50d) produced as a gaseous oxygen product under medium pressure (MP GOX). The second part stream 2a of the feed air is substantially fully liquefied in the liquefaction chamber of the secondary condenser. The liquefied second part stream 2b is introduced into the evaporation chamber of the head condenser 14 of the precolumn 10.
In order to produce a highly pure nitrogen product, many separation stages are needed in the corresponding column. In the case of the method of the invention, it is particularly favorable to produce the highly purified pressurized nitrogen from the precolumn as, in the case of the arrangement of columns and condensers shown in the drawing, the space above the secondary condenser can still be utilized effectively. The height of the entire rectification coldbox is determined anyway by the (large) height of that of the double column part. The pressurized nitrogen product from the high-pressure column can then comprise a lower purity.
Both condensers 14 and 46 of the exemplary embodiments are realized as bath evaporators, at least one plate heat exchanger block being arranged in a liquid bath.
| Number | Date | Country | Kind |
|---|---|---|---|
| 12008635.0 | Dec 2012 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2013/003929 | 12/20/2013 | WO | 00 |
