阅读说明：本技术 用于低温分离空气的方法和设备 (Method and apparatus for the cryogenic separation of air ) 是由 斯特凡·洛克纳 于 2019-08-20 设计创作，主要内容包括：本发明涉及一种使用空气分离设备来低温分离空气的方法,所述空气分离设备具有蒸馏柱系统(100),所述蒸馏柱系统具有第一分离单元、第二分离单元、第三分离单元和第四分离单元(110-140)。将压缩并且冷却后的空气送入所述第一分离单元(110)之中,所述第一分离单元(110)以4至9bar绝对压力的第一压力水平运行,所述第二分离单元、第三分离单元和第四分离单元(120-140)以1至3bar绝对压力的第二压力水平运行,借助所述第一分离单元(110)形成富氧且贫氮、含氩的第一底盘液体和富氮且贫氧的第一顶部气体,将所述第一底盘液体至少部分地转移到所述第四分离单元(130)之中,将所述第一顶部气体至少部分地液化并且送回到所述第一分离单元(110),借助所述第二分离单元(120)形成富氧的第二底盘液体和富氩的第二顶部气体,将所述第二顶部气体第一部分转移到所述第三分离单元(130)中并且将第二部分转移到所述第四分离单元(140)之中,借助所述第三分离单元(130)将供应给所述蒸馏柱系统(100)的总空气量中所含的氩的至少大部分分离出来,并且借助所述第三分离单元(130)将液态回流提供给所述第二分离单元(120),借助所述第四分离单元(140)形成第四底盘液体和第四顶部气体,并且将所述第四底盘液体至少部分地送回到所述第二分离单元(120)。所述第二分离单元(120)具有10至50个理论板,所述第三分离单元(130)具有10至60个理论板,所述第三分离单元(130)布置在所述第二分离单元(120)上方并且所述第四分离单元(140)布置在所述第一分离单元(110)旁边。所述第三分离单元(130)在下方区域中相对于所述第二分离单元(120)的上方区域开口,或者所述第三分离单元(130)通过在所述第二分离单元(120)的上方区域与所述第三分离单元(130)的下方区域之间延伸的管道与所述第二分离单元(120)相连。本发明还涉及一种对应的设备(200)。(The invention relates to a method for the cryogenic separation of air using an air separation plant having a distillation column system (100) with a first separation unit, a second separation unit, a third separation unit and a fourth separation unit (110-140). Feeding the compressed and cooled air into the first separation unit (110), the first separation unit (110) operating at a first pressure level of 4 to 9bar abs, the second, third and fourth separation units (120) operating at a second pressure level of 1 to 3bar abs, forming an oxygen-rich and nitrogen-poor, argon-containing first tray liquid and a nitrogen-rich and oxygen-poor first overhead gas by means of the first separation unit (110), at least partially transferring the first tray liquid into the fourth separation unit (130), at least partially liquefying and returning the first overhead gas to the first separation unit (110), forming an oxygen-rich second tray liquid and an argon-rich second overhead gas by means of the second separation unit (120), transferring a first part of the second overhead gas into the third separation unit (130) and transferring a second part into the second separation unit (130) -among the four separation units (140), -separating at least a major part of the argon contained in the total amount of air supplied to the distillation column system (100) by means of the third separation unit (130), and-providing a liquid reflux to the second separation unit (120) by means of the third separation unit (130), -forming a fourth bottom liquid and a fourth top gas by means of the fourth separation unit (140), and-returning the fourth bottom liquid at least partly to the second separation unit (120). The second separation unit (120) has 10 to 50 theoretical plates, the third separation unit (130) has 10 to 60 theoretical plates, the third separation unit (130) is arranged above the second separation unit (120) and the fourth separation unit (140) is arranged beside the first separation unit (110). The third separation unit (130) is open in a lower region relative to an upper region of the second separation unit (120), or the third separation unit (130) is connected to the second separation unit (120) by a conduit extending between the upper region of the second separation unit (120) and the lower region of the third separation unit (130). The invention also relates to a corresponding device (200).)

1. A method for the cryogenic separation of air using an air separation plant having a distillation column system (100) with a first separation unit (110), a second separation unit (120), a third separation unit (130) and a fourth separation unit (140), wherein compressed and cooled air is fed into the first separation unit (110), the first separation unit (110) is operated at a first pressure level of 4 to 9bar absolute, the second separation unit (120), the third separation unit (130) and the fourth separation unit (140) are operated at a second pressure level of 1 to 3bar absolute, an oxygen-rich and nitrogen-poor, an argon-containing first bottom liquid and a nitrogen-rich and oxygen-poor first top gas are formed by means of the first separation unit (110), the first bottom liquid is partially or completely transferred into the fourth separation unit (130), partially or completely liquefying and returning the first top gas to the first separation unit (110), forming an oxygen-rich second bottom liquid and an argon-rich second top gas by means of the second separation unit (120), transferring a first part of the second top gas into the third separation unit (130) and a second part into the fourth separation unit (140), partially or completely separating off the argon contained in the total amount of air supplied to the distillation column system (100) by means of the third separation unit (130), providing a liquid reflux to the second separation unit (120) by means of the third separation unit (130), forming a fourth bottom liquid and a fourth top gas by means of the fourth separation unit (140), and partially or completely returning the fourth bottom liquid to the second separation unit (120), characterized in that the second separation unit (120) has 10 to 50 theoretical plates, the third separation unit (130) has 10 to 60 theoretical plates, the third separation unit (130) is arranged above the second separation unit (120), the fourth separation unit (140) is arranged beside the first separation unit (110), and the third separation unit (130) is open in a lower region with respect to an upper region of the second separation unit (120), or the third separation unit (130) is connected to the second separation unit (120) by a conduit extending between an upper region of the second separation unit (120) and a lower region of the third separation unit (130).

2. The method of claim 1, wherein a lower terminal of the fourth separation unit (140) is disposed no more than eight meters above a lower terminal of the first separation unit (110).

3. Method according to one of the preceding claims, wherein the compressed and cooled air fed into the first separation unit comprises a gaseous and liquefied inlet gas stream (1, 2).

4. The method according to one of the preceding claims, wherein the first separation unit (110) and the second separation unit (120) are arranged within one common column housing or in two structurally connected column housings, wherein the common column housing or the column housing of the second separation unit (120) is structurally connected to the third separation unit (130).

5. The method according to one of the preceding claims, wherein the fourth separation unit has 18 to 55 theoretical plates.

6. The method of one of the preceding claims, wherein the first portion of the second top gas comprises 20% to 60% volume percent of the second top gas and the second portion of the second top gas comprises 40% to 80% volume percent.

7. The method according to one of the preceding claims, wherein the fourth chassis liquid is fed back into the second separation unit (120) using a transfer pump (170) or using two or more transfer pumps arranged in parallel.

8. Method according to one of the preceding claims, wherein the first separation unit (110), the second separation unit (120) and the third separation unit (130) are arranged in one common cold box (a).

9. The method according to claim 8, wherein the fourth separation unit (140) is arranged in the common cold box (A) or in another cold box (B).

10. Method according to claim 9, wherein the first separation unit (110), the second separation unit (120) and the third separation unit (130) on the one hand and the fourth separation unit (140) on the other hand are interconnected and/or with other equipment by means of a sectionally vertically extending duct (20), wherein the duct (20) is at least partly arranged in a separate duct cold box (C).

11. Method according to claim 10, wherein a subcooler (120) is furthermore arranged in the pipe cold box (C).

12. The process according to one of the preceding claims, wherein liquid air product is withdrawn from the distillation column system (100), increased in pressure in the liquid state, converted into the gaseous or supercritical state by heating, and discharged from the air separation plant.

13. An air separation plant having a distillation column system (100) with a first separation unit (110), a second separation unit (120), a third separation unit (130) and a fourth separation unit (140), wherein the air separation plant is adapted to feed compressed and cooled air into the first separation unit (110), the first separation unit (110) being operated at a first pressure level of 4 to 9bar absolute, the second separation unit (120), the third separation unit (130) and the fourth separation unit (140) being operated at a second pressure level of 1 to 3bar absolute, an oxygen-rich and nitrogen-poor, an argon-containing first bottom tray liquid and a nitrogen-rich and oxygen-poor first top gas being formed by means of the first separation unit (110), the first bottom tray liquid being partly or completely transferred into the fourth separation unit (130), partially or completely liquefying and returning the first top gas to the first separation unit (110), forming an oxygen-rich second bottom liquid and an argon-rich second top gas by means of the second separation unit (120), transferring a first part of the second top gas into the third separation unit (130) and a second part into the fourth separation unit (140), partially or completely separating off the argon contained in the total amount of air supplied to the distillation column system (100) by means of the third separation unit (130), providing a liquid reflux to the second separation unit (120) by means of the third separation unit (130), forming a fourth bottom liquid and a fourth top gas by means of the fourth separation unit (140), and returning the fourth bottom liquid at least partially to the second separation unit (120), characterized in that the second separation unit (120) has 10 to 50 theoretical plates, the third separation unit (130) has 10 to 60 theoretical plates, the third separation unit (130) is arranged above the second separation unit (120), the fourth separation unit (140) is arranged beside the first separation unit (110), and the third separation unit (130) is open in a lower region with respect to an upper region of the second separation unit (120), or the third separation unit (130) is connected to the second separation unit (120) by a conduit extending between an upper region of the second separation unit (120) and a lower region of the third separation unit (130).

Background

The production of liquid or gaseous air products by cryogenic separation of air in air separation plants is known and is for example published by Wiley-VCH, inc 2006, by h.The editorial published "Industrial Gases Processing" book is described in particular in section 2.2.5 "Cryogenic Rection".

The air separation plant has distillation column systems which can be designed, for example, as a two-column system, in particular as a typical linde two-column system, but also as a three-column or multi-column system. In addition to the distillation column for extracting liquid and/or gaseous nitrogen and/or oxygen, i.e. for nitrogen-oxygen separation, a distillation column for extracting other air components, in particular krypton, xenon and/or argon, may be provided.

The distillation columns of the distillation column system are operated at different pressure levels. Known two-column systems have a so-called high-pressure column (also referred to as pressure column, medium-pressure column or lower column) and a so-called low-pressure column (also referred to as upper column). The high-pressure column is typically operated at a pressure level of 4 to 7bar, in particular about 5.3 bar. The low-pressure column is typically operated at a pressure level of 1 to 2bar, in particular about 1.4 bar. In some cases, higher pressure levels may also be used in the low pressure column. The pressures described here and below are the absolute pressures at the top of the respective given column.

In the known method and apparatus for the cryogenic separation of air, an oxygen-enriched and nitrogen-depleted liquid is formed in the lower region of the high-pressure column and is withdrawn from the high-pressure column. The liquid, which in particular also contains argon, is at least partly fed into the low-pressure column and the separation is continued there. The liquid may be partially or completely vaporized before it is fed into the low pressure column, where vaporized and non-vaporized portions may be fed into the low pressure column at different locations where appropriate.

The invention is based on a method or a corresponding device in which a high-pressure column and a low-pressure column are used. However, in the context of the present invention, the low-pressure column is not designed in one piece, but is divided into a first section and a second section, wherein the first section and the second section are arranged at different positions and at different heights of the air separation plant and in particular do not project in an overlapping manner in a top view of the longitudinal axis of the column. However, in the context of the present invention, the first section and the second section of the low pressure column are operated at the same pressure level. The low-pressure column used in the context of the present invention, which is divided into two sections, is thus distinguished from the likewise known arrangement in which, in addition to the high-pressure column and the low-pressure column, a further column for separating nitrogen and oxygen is provided, which column however operates at a pressure level which is between the pressure levels at which the high-pressure column and the low-pressure column operate.

For extracting argon, an air separation plant having a crude argon column and a pure argon column may be used.An embodiment is shown in FIG. 2.3A of the book (see above) and described in the section "retrieval in the Low-pressure, CRude and Pure Argon Column" from page 26 and in the section "Cryogenic Production of Pure Argon" from page 29. As described therein, argon accumulates in the corresponding apparatus at a certain height in the low-pressure column. At this or another advantageous location, where appropriate also below the argon maximum, the so-called argon transition point, argon-enriched gas, with an argon concentration of typically 5 to 15 mole percent, is withdrawn from the low-pressure column and transferred into the original argon column. The corresponding gas typically contains about 100ppm nitrogen, otherwise essentially oxygen.

The original argon column is used primarily to separate oxygen from the gas withdrawn from the low pressure column. The oxygen separated in the original argon column or the corresponding oxygen-enriched fluid can be fed back in fluid form into the low-pressure column. Here, oxygen or an oxygen-enriched fluid is fed into the low-pressure column, typically at a number of theoretical or actual plates below the feed point of the liquid withdrawn from the high-pressure column, enriched in oxygen and depleted in nitrogen, and, where appropriate, partially or completely vaporized. The gaseous fraction, which remains in the original argon column during the separation, and which contains mainly argon and nitrogen, is further separated in a pure argon column to obtain pure argon. The crude argon column and the pure argon column have overhead condensers which can be cooled, in particular, by a portion of the oxygen-enriched and nitrogen-depleted liquid withdrawn from the high-pressure column, which partially evaporates on cooling. Other fluids may be used for cooling.

In principle, a pure argon column can also be omitted in the corresponding apparatus, wherein here it is typically ensured that the nitrogen content at the argon transition is below 1 ppm. In this case, the argon withdrawn from the crude argon column, at a point below the fluid conventionally transferred into the pure argon column, is of the same quality as the argon withdrawn from the conventional pure argon column, wherein the crude argon condenser, i.e. the plate in the section between the overhead condenser of the crude argon column and the corresponding suction device, serves as a barrier for nitrogen.

And(see above) although the argon content in the atmosphere is below 1 mole percent, it has a large effect on the concentration profile in the low pressure column as described with reference to figure 2.4A. The separation in the lowermost separation section of the low pressure column, typically comprising 30 to 40 theoretical or actual plates, can therefore be considered as a substantially binary separation between oxygen and argon. Only from the outlet position of the gas transferred into the original argon column will the separation within a few theoretical or actual plates be converted into a ternary separation of nitrogen, oxygen and argon.

Thus, even if an extraction of argon should not be carried out in the corresponding apparatus or the corresponding method, it may prove advantageous to discharge argon from the low-pressure column. As already mentioned, a corresponding argon discharge takes place when using the original argon column, since the argon-rich gas is transferred from the low-pressure column into the original argon column, but essentially only the oxygen contained in this gas is returned into the low-pressure column. In contrast, the argon discharged with the correspondingly extracted gas is continuously withdrawn from the low-pressure column.

By "argon tapping" is generally meant here the measure of transferring the argon-containing fluid from the low-pressure column into another separation unit and after depletion of the argon partly or completely returning it from the other separation unit into the low-pressure column. The classical way of argon venting is to use a raw argon column. However, an argon purge column described below may also be used.

The advantageous effect of argon purging is due to the fact that there is no longer a need to separate oxygen and argon in the low pressure column for the amount of argon purged, but rather such a binary separation can be diverted from the low pressure column. In principle, separation of oxygen and argon in the low pressure column is itself cumbersome and requires a corresponding "heating" power of the main condenser. By venting argon from the low pressure column, the heating power of the main condenser can be reduced. Thus, with the oxygen production remaining constant, for example, either more air can be injected into the low pressure column or more compressed nitrogen can be withdrawn from the high pressure column, each of which can provide an energy advantage.

In a conventional raw argon column, as explained, raw argon is extracted and purified to pure argon in a downstream pure argon column. In contrast, the argon tapping column is primarily used for argon tapping, in order to improve the separation in the low-pressure column. By an "argon discharge column" is understood here in principle a separation column for separating oxygen and argon, which separation column is not intended for extracting pure argon product, but is essentially intended for discharging argon from the low-pressure column.

The construction of the argon discharge column differs only slightly from that of a conventional crude argon column in principle. However, the argon discharge column typically contains much fewer theoretical or actual plates, i.e. less than 40, in particular between 15 and 30. For further values of the number of plates reference is made to the following detailed description. As in the case of conventional crude argon columns, the bottom region of the argon outlet column can usually be connected in particular to the middle of the low-pressure column. In particular, the argon discharge column may be cooled by means of an overhead condenser in which the oxygen-rich and nitrogen-depleted liquid withdrawn from the high-pressure column is partially evaporated. The argon discharge column typically does not have a floor vaporizer. The present invention uses an argon discharge column arranged in the following manner.

US 5339648A discloses an air separation plant having a high pressure column and a low pressure column divided vertically in one section. The low-pressure column section formed in this section can thus be used to discharge argon. According to US 5311744 a, the entire argon column is located on a high-pressure column. Below the argon column there is a further separation section, above which a fluid is withdrawn and sent to a nitrogen stripper. FR 2739438 a1 discloses a distillation column system having a two-part low pressure column with an argon column standing next to the assembly.

The object of the invention is to improve the cryogenic separation of air using an argon discharge column and to design the arrangement of the distillation column used in a particularly advantageous manner.

Disclosure of Invention

Against this background, the invention proposes a method for the cryogenic separation of air and a corresponding plant having the features of the respective independent claims. Embodiments are the subject matter of the respective dependent claims and the following description.

Before explaining the features and advantages of the present invention, some basic principles of the present invention are further explained and the terms used below are defined.

Apparatus for use in air separation plants of the specialist literature cited, e.g. in(see above) in the book in section 2.2.5.6 "Apparatus". Thus, unless the following definitions deviate therefrom, the words in the context of this application make explicit reference to the cited technical documents.

In the language used herein, fluids and gases may be enriched or depleted in one or more components, where "enriched" may mean a content of at least 50%, 75%, 90%, 95%, 99%, 99.5%, 99.9%, or 99.99% on a molar, weight, or volume basis, and "depleted" may mean a content of up to 50%, 25%, 10%, 5%, 1%, 0.1%, or 0.01%. The concept of "mostly" may correspond to the definition of "rich". Additionally, liquids and gases may be enriched or depleted in one or more components, where these concepts refer to the content in the initial liquid or initial gas from which the liquid or gas was extracted. A liquid or gas is "enriched" if it contains at least 1.1 times, 1.5 times, 2 times, 5 times, 10 times, 100 times or 1,000 times the content of the corresponding component relative to the initial liquid or initial gas, and "depleted" if it contains at most 0.9 times, 0.5 times, 0.1 times, 0.01 times or 0.001 times the content of the corresponding component. If reference is made here, for example, to "oxygen", "nitrogen" or "argon", this is also to be understood as a liquid or gas which is rich in oxygen or nitrogen, but which does not necessarily consist entirely of these substances.

The present application uses the two concepts "pressure level" and "temperature level" to characterize pressure and temperature, thereby indicating that it is not necessary to use the respective pressure and temperature in the form of precise pressure or temperature values in the corresponding device in order to implement the inventive concept. However, such pressures and temperatures typically move within a range, for example, of the mean ± 1%, 5%, or 10%. The respective pressure and temperature levels can be in non-intersecting ranges or in overlapping ranges. In particular, for example, the pressure level includes an unavoidable or expected pressure loss. The corresponding applies to the temperature level. The pressure level in bar here is absolute pressure.

The high-pressure column and the low-pressure column of the air separation plant (or the first section of the low-pressure column in the context of the present invention) are in heat exchange connection by means of a so-called main condenser. The main condenser may in particular be arranged in the lower (floor) region of the low-pressure column (or here the first section thereof). In this case, a so-called built-in main condenser is involved and the evaporation chamber of the main condenser is at the same time the inner chamber of the low-pressure column (or the first section thereof). However, the main condenser, the so-called external main condenser, can in principle be arranged outside the interior of the high-pressure column.

The main condenser and the overhead condenser of the argon discharge column used in the context of the present invention can each be designed as a condenser evaporator. "condenser evaporator" refers to a heat exchanger in which a first condensing fluid stream is indirectly heat exchanged with a second evaporating fluid stream. Each condenser-evaporator has a liquefaction chamber and an evaporation chamber with a liquefaction or evaporation channel. The first fluid stream is condensed (liquefied) in the liquefaction chamber and the second fluid stream is vaporized in the vaporization chamber. The vaporization chamber and the liquefaction chamber are formed by a set of channels in heat exchange relationship with each other. In particular, the main condenser can be designed as a single-layer or multilayer submerged evaporator, in particular as a cascade evaporator (as described, for example, in EP 1287302B 1), but alternatively as a falling-film evaporator. The main condenser may be formed by a single heat exchanger module or a plurality of heat exchanger modules arranged in the same pressure vessel. The invention is, however, expressly not limited to a corresponding type of condenser evaporator or condenser.

The distillation column system of the air separation plant is arranged in one or more cold boxes. By "cold box" is understood here an insulated enclosure comprising an insulated interior with an outer wall in its entirety, except for the insulating sleeves of the pipes and the like. In which are arranged the components of the apparatus that need to be insulated, such as one or more distillation columns and/or heat exchangers. The insulating effect can be achieved by corresponding outer wall embodiments and/or by filling the gap between the device component and the outer wall with an insulating material. For the latter variant, it is preferable to use a pulverulent material, such as perlite. In a typical air separation plant, not only the distillation column system of the plant for the cryogenic separation of air, but also the main heat exchanger and other cryogenic plant components are surrounded by one or more cold boxes. The external dimensions of the cold box generally determine the transport dimensions of the prefabricated unit.

The "main heat exchanger" of the air separation plant is used to cool the feed gas in indirect heat exchange with the reflux stream in the distillation column system. The main heat exchanger may be formed by a single or a plurality of heat exchanger sections in parallel and/or in series, for example by one or more plate heat exchanger groups. Individual heat exchangers dedicated to the evaporation or pseudo-evaporation of a single liquid or supercritical fluid without heating and/or evaporating another fluid are not part of the main heat exchanger.

In the language used herein, a "subcooler" or "ultra-low temperature counter-current heat exchanger" (the terms are used fully interchangeably hereinafter) is a heat exchanger through which gaseous and liquid streams are passed in heat exchange relationship with each other in an air separation plant, the streams being withdrawn from a rectification column system and partially or fully returned to the rectification column system after heat exchange.

The relative spatial concepts of "upper", "lower", "above", "below", "above …", "below …", "beside …", "side-by-side", "vertical", "horizontal", and the like, relate herein to the spatial orientation of the distillation columns of an air separation plant in normal operation. The arrangement of two distillation columns or other components "one above the other" is to be understood here to mean that the upper end of the lower of the two installation parts is at a lower or the same geodetic height than the lower end of the upper of the two installation parts, and the projections of the two installation parts coincide in the horizontal plane. In particular, the two device parts are arranged exactly one above the other, i.e. the axes of the two device parts run on the same vertical straight line. In other cases, however, it may also be advantageous not to arrange the axes one above the other, in particular when the equipment components have different diameters, for example in order to arrange the equipment components with the smaller diameter closer to the cold box wall.

THE ADVANTAGES OF THE PRESENT INVENTION

The invention is based on the recognition that: the arrangement of the argon discharge column in the distillation column system of an air separation plant with a two-part low-pressure column in a manner which is clearly different from the prior art makes it possible to carry out the air separation process particularly effectively and, in particular, to build up a corresponding air separation plant in a particularly simple and cost-effective manner.

The advantages which can be achieved in the context of the present invention include in particular the possibility of arranging the respective components of the distillation column system proposed according to the invention in a particularly advantageous manner in different cold boxes which can be prefabricated even in the case of argon tapping columns and can be transported to the respective place of use after prefabrication. The advantages of the invention are not, however, limited to the improved disposability and transportability of the components in the cold box, but in particular also include the possibility of constructing corresponding air separation plants in a simple manner, since a large number of pipelines, which are typically required when, for example, an argon discharge column is arranged in a different conventional manner, are dispensed with.

In addition to the bisection of the low-pressure column described above, an important aspect of a particularly preferred embodiment of the present invention is that the argon discharge column is placed on the lower section of the corresponding two-way low-pressure column with the lower side open. In the context of the present application, the "lower section" or "first section" of a two-part low pressure column generally refers to that section in the bottom tray thereof which forms an oxygen-rich liquid as in the bottom tray of a conventional one-piece low pressure column. In another preferred embodiment, however, the argon withdrawal column can also be connected to the lower section of the two-part low-pressure column via a line. In all embodiments of the invention, the argon withdrawal column is disposed above the lower portion of the low pressure column.

In this case, the lower or first section of the respective two-part low-pressure column can be connected as a structural unit to the high-pressure column. In particular, the main condenser, which connects the high-pressure column and the low-pressure column in a heat-exchanging manner, is also located in the first or lower section of the two-part low-pressure column. In contrast, the "second section" or "upper section" of the two-part low pressure column is that section in which a nitrogen-rich top gas is formed on the top side, which top gas can be output as the corresponding (low pressure) nitrogen product. In the context of the present invention, the low-pressure column is in particular suitably divided into two such that a maximum of the argon concentration is produced in the upper region or at the top of the first or lower section of the two-part low-pressure column, which corresponds to the region of maximum argon concentration in conventional one-piece low-pressure columns. This is achieved in particular by a corresponding selection of the number of theoretical plates in the first part or lower section of the low-pressure column and known structural measures.

By means of the arrangement proposed according to the invention of the high-pressure column, the first section of the low-pressure column and the argon outlet column, it is possible in particular to arrange the respective structural unit realized into a cold box which is still transportable, so that the respective air separation plant can be prefabricated and, if necessary, the respective cold box can be brought to the respective place of use. The remaining components in the low temperature section of the air separation plant, particularly the second section of the low pressure column and, if necessary, the ultra-low temperature counter-flow heat exchanger, may each be transferred into at least one second cold box, which typically also does not exceed the maximum size available for transport to the point of use. A particularly advantageous embodiment of the invention results if the second section of the low-pressure column is transferred into a certain cold box and the line for the pipe installation of the separation unit is transferred, in particular together with a subcooler, into another cold box.

In summary, the present invention provides a process for the cryogenic separation of air using an air separation plant having a distillation column system. In the context of the present invention, a distillation column system comprises a first separation unit (corresponding to the high pressure column of a conventional air separation plant), a second separation unit (corresponding to the first or lower section of a two-part low pressure column), a third separation unit (corresponding to an argon withdrawal column) and a fourth separation unit (corresponding to the second or upper section of a two-part low pressure column). In the context of the present invention, the compressed and cooled air is fed to the first separation unit, but not necessarily only to the separation unit. The corresponding air can be compressed by known measures, in particular using a main air compressor, if necessary one or more secondary compressors, superchargers, etc. In the context of the present invention, it is purified by means of measures known as such, in particular to remove water and carbon dioxide. In the context of the present invention, different measures can be used for air purification and cooling, and for further processing of the air. In particular, one or more pressure reducing valves, superchargers, turbines, etc. may also be used, as these are basically known in the field of air separation. Details are again referred to in the relevant technical literature, e.g.(see above).

In the context of the present invention, the first separation unit is operated at a first pressure level of 4 to 9bar absolute, in particular 4 to 8bar absolute, for example a pressure level of about 5.3bar absolute, corresponding to the normal operating pressure of the high-pressure column of the air separation plant. In the context of the present invention, the second separation unit, the third separation unit and the fourth separation unit are, in contrast, operated at a common second pressure level, which in the context of the present invention is 1 to 3bar, in particular 1 to 2bar absolute, i.e. corresponds to the typical pressure level of a low-pressure column of an air separation plant. The second pressure level may be, for example, about 1.4bar absolute.

In the context of the present invention, as is known for high-pressure columns of air separation plants, an oxygen-rich and nitrogen-lean, argon-containing first bottom liquid and a nitrogen-rich and oxygen-lean first top gas are formed by means of a first separation unit. For further details, reference is also made to the relevant technical literature on air separation or on operating the high-pressure columns of known air separation plants.

In the context of the present invention, the first bottom tray liquid is partly or completely transferred to the fourth separation unit and the first top gas is partly or completely liquefied and returned to the first separation unit. In particular, for liquefying the first top gas or its part which is fed back to the first separation unit, a main condenser is used which in this case connects the first separation unit and the second separation unit in a heat-exchanging manner. Further details regarding the corresponding main condenser are described below.

The invention is not limited to liquefying only the first overhead gas portion that is returned to the first separation unit. Rather, in the context of the present invention, other top gases can also be liquefied and discharged as product from the air separation plant, in particular as liquid air product, without or with subsequent evaporation or transition to a supercritical state. In the context of the present invention, it is also possible to pass the further liquefied top gas, i.e. the liquefied first top gas, from the top of the first separation unit to the fourth separation unit as a return flow, in particular after having previously fed the corresponding liquefied top gas to be conducted through the ultra-low temperature counter-flow heat exchanger. The unliquefied overhead gas may also be withdrawn from the top of the first separation unit and output from the air separation plant, for example as a compressed nitrogen product. As previously mentioned, by using an argon discharge column, in particular the amount of high pressure column overhead gas discharged from the air separation plant can be increased.

In the context of the present invention, an oxygen-rich second bottom liquid and an argon-rich second top gas are formed by means of a second separation unit. This may for example have an argon content of 5% to 15% and essentially oxygen in the remainder. As already mentioned, in the context of the present invention, the second separation unit essentially corresponds to the lower section or first section of a two-part low-pressure column, or to the lower part of a conventional one-piece low-pressure column up to the argon maximum. As also previously mentioned, this can be achieved by selecting the corresponding separating agent or selecting the number of separating plates. The corresponding design of the second separation unit makes it possible to discharge argon in the third separation unit in an advantageous manner.

In the context of the present invention, for this purpose the first portion of the second top gas is transferred into a third separation unit and the second portion into a fourth separation unit. The fourth separation unit corresponds to the conventional second or upper section of the two-part low-pressure column, while the third separation unit is essentially provided for the argon discharge. As described below, the third separation unit together with the second separation unit can be designed as a structural unit in the context of the present invention. Thus, in this case there is no need to output the corresponding fluid from the low pressure column and transfer it to the argon discharge column. But instead the second top gas is transferred in this embodiment to the third separation unit, in particular without being diverted. In this embodiment, the transfer is carried out in particular without a line.

At least a major part of the argon contained in the total amount of air supplied to the distillation column system is separated off by means of a third separation unit, wherein a liquid reflux stream which is returned to the second separation unit is produced by means of the third separation unit. To this end, the third separation unit has separation zones which can be formed using known separation devices, in particular ordered or disordered packings or plates. For the dimensioning of the third separation unit, reference is made to the following explanations. In principle, the third separation unit can be designed in a known manner, wherein the third separation unit corresponds to an argon outlet column which is open in the lower region relative to the second separation unit.

In the context of the present invention, a fourth bottom liquid and a fourth top gas are formed by means of a fourth separation unit and the fourth bottom liquid is partly or completely returned to the second separation unit. According to the invention, the fourth separation unit is arranged beside the first (and thus also the second, if necessary) separation unit, so that in particular a suitable pump is used to transfer the fourth chassis liquid to the second separation unit.

In the context of the present invention, it is provided in particular that the second separation unit, i.e. the first or lower section of the low-pressure column, has 10 to 50 theoretical plates, in particular 20 to 40 theoretical plates. In the context of the present invention, the third separation unit has 10 to 60 theoretical plates, in particular 15 to 30 theoretical plates. The second separation unit is thus a low-pressure column section comprising a typical oxygen section or a corresponding separation device of this type of oxygen section. In contrast, the third separation unit is designed as an argon outlet column as explained in more detail. In particular, the third separation unit may have a diameter of at most 80%, 70%, 60% or 50% of the diameter of the second separation unit.

In the context of the present invention, it is furthermore provided that a third separating unit (in the sense explained above) is arranged above, in particular just above, the second separating unit and the third separating unit is open in a lower region, in particular not conically, relative to the upper region of the second separating unit, or the third separating unit is connected to the second separating unit by a line extending between the upper region of the second separating unit and the lower region of the third separating unit. Here, the opening of the third separation unit which is "not tapered" means that the column shell of the third separation unit has no narrowed portion relative to the column shell of the second separation unit. In particular, in the context of the present invention, there is no cross-sectional reduction relative to the cross-sectional area of the third separation unit in this embodiment. In particular, however, the third separation unit may, as already mentioned, have a smaller cross section than the second separation unit, and the entire cross section of the third separation unit may be available for the first portion of the second top gas to flow into the third separation unit. In contrast to the conventional arrangement in which the argon withdrawal column is arranged beside the distillation column system composed of the high-pressure column and the low-pressure column, in the context of the present invention, even if in one embodiment a line extends between the upper region of the second separation unit and the lower region of the third separation unit, no corresponding fluid has to be transferred by means of pumps, lines or the like. Conversely, the second overhead gas from the second separation unit may rise substantially unimpeded into the third separation unit and the liquid from the third separation unit may flow substantially unimpeded out into the second separation unit. This can be achieved in particular without a diversion or without a line if the third separating unit is open in the lower region relative to the upper region of the second separating unit. As previously mentioned, a particular advantage of the present invention is also herein.

For the sake of completeness only, it is emphasized again that in the context of the present invention, the first separation unit and the second separation unit are also arranged one above the other, otherwise also as explained above and below.

In this connection, as is known for argon tapping columns, the argon tapping column used in the context of the present invention, i.e. the third separation unit, may also have an overhead condenser which may be cooled with oxygen-enriched liquid from the high-pressure column, here the first bottom liquid. The corresponding liquid which partially evaporates on cooling can then be fed into the fourth separation unit, in particular at different heights. Advantageously, the corresponding streams are split outside the overhead condenser, so that they have different concentrations.

In the context of the present invention, as already mentioned, it is possible in particular to use falling-film evaporators or cascade evaporators, in particular multilayer cascade evaporators, of the type described above as main condensers, i.e. as condensers which connect the first separation unit and the second separation unit in a heat-exchanging manner. In this way, a particularly efficient liquefaction takes place in the corresponding main condenser. However, the invention is expressly not limited to this form of condenser evaporator, but may be used with any type of main condenser.

In the context of the present invention, the compressed and cooled air fed into the first separation unit may in particular comprise gaseous and liquefied inlet streams, which may each be fed into the first separation unit at a first pressure level. In this case, the gaseous feed stream can be fed into the first separation unit at a first feed position and the liquid feed stream can be fed into the first separation unit at a second feed position, wherein the first feed position is located below the second feed position, wherein no separation device is typically provided in the first separation unit below the first feed position, wherein the second feed position is advantageously above a liquid retention device from which the liquid stream can be withdrawn from the first separation unit, and wherein the second feed position is above a certain separation unit or a certain separation region of the first separation device. It should be explicitly emphasized that in the context of the present invention, it is also possible to feed the inlet gas into the first separation unit, for example in two stages, in a common line. In the field of air separation, it is known to form the corresponding material streams.

It is particularly advantageous in the context of the present invention if the first separation unit and the second separation unit are structurally connected to one another and can be arranged within a common column housing, wherein the common column housing can also be structurally connected to the third separation unit. The common housing according to the invention can in particular be a common cylindrical outer container, so that the first and second separating units in the context of the invention can be manufactured with the same cross section. If the high-pressure column or the first separating unit has a smaller diameter than the first section or the second separating unit of the low-pressure column, it is typically not arranged in a common column housing; the column shell of the high-pressure column is mounted on the bottom side of the column shell of the low-pressure column root section. In this case, then, the first separation unit and the second separation unit typically have separate, but interconnected, column housings. In principle, different cross-sections can also be used. The third separating element has in particular a smaller cross section than the first separating element and/or the second separating element and therefore does not have to be arranged within this common cylindrical housing, but if the third separating element is open in the lower region relative to the upper region of the second separating element, it is connected, for example welded, to the common housing of the first separating element and the second separating element or to the housing of the second separating element. In this case, a pipeless direct contact of the column shells of the second and third separation units is generally provided. As previously described, but may also be provided as connected by tubing.

The fourth separation unit is advantageously not structurally connected to the first, second and third separation units as such, but is connected to the first, second and third separation units only by piping or tubing. In this way, it is possible on the one hand to arrange the first, second and third separation units and, on the other hand, the fourth separation unit at different locations of the corresponding apparatus and, in particular, to arrange them in different cold boxes. In this case, the fourth separating element can likewise have a smaller, but possibly also larger, cross section than the second separating element. In particular, the fourth separation unit may have 18 to 65 theoretical plates and thus correspond to the remaining part of the corresponding two-part low-pressure column of which the first section is constituted by the second separation unit.

In the method proposed by the invention, the first part of the second top gas has in particular a volume percentage of 20% to 50% of the second top gas and the second part of the second top gas has a volume percentage of 50% to 80% (and thus in particular the remaining part). In this way, in the context of the present invention, a particularly effective argon discharge is produced in the third separation unit.

As already mentioned, in the context of the present invention, the fourth separation unit is arranged beside the first separation unit and here in particular in a separate cold box. In this way, the overall height of the corresponding air separation plant is reduced overall. In such an embodiment, provision is made in particular for the fourth chassis liquid to be returned to the second separation unit using a feed pump or at least two feed pumps arranged in parallel and to be passed back to the second separation unit here in particular as a liquid return stream at the top of the second separation unit. In particular, two pumps may be operated in parallel and a third pump may be provided for redundancy reasons. The use of two feed pumps arranged in parallel makes it possible to construct in a particularly simple manner, since standard pumps of corresponding dimensions are available. In this case, a corresponding feed pump is provided for overcoming the height difference between the second separation unit and the fourth separation unit, and vice versa. Conversely, the second portion of the second top gas may advantageously flow into the fourth separation unit with a minimum pressure difference between the second separation unit and the fourth separation unit.

In particular, the fourth separation unit is suitably arranged beside the first separation unit such that the lower terminal of the fourth separation unit is arranged no more than eight meters, in particular no more than seven, six or five meters, for example one to four meters, above the lower terminal of the first separation unit. Here, the "lower terminal end" is a part of the separation unit, i.e. the column chassis that forms the boundary of the column cavity. But also a line leads from there. In particular, the fourth separating unit is arranged on a support at said level to ensure that the pump used has a sufficient cavitation margin. By such an arrangement, an air separation plant can be built which is particularly compact and of limited vertical extent.

As already mentioned several times, the first, second and third separating units are advantageously arranged in a common cold box and the fourth separating unit is arranged in another cold box.

In the context of the present invention, the first, second and third separation units on the one hand and the fourth separation unit on the other hand are in particular connected to each other and/or to other equipment by means of pipes. At least a portion of the conduit may extend vertically. In the context of the present invention, at least a part of such a pipe may be arranged in one additional cold box, herein referred to as "pipe cold box", which may be prefabricated, independently of the two cold boxes in which the first, second and third separation units are arranged on the one hand and the fourth separation unit on the other hand. The provision of corresponding pipe cold boxes enables a corresponding reduction in the size of the other two cold boxes and in particular enables these cold boxes to be designed in a (better) transportable manner. Most of the instruments, valves, etc. may also be placed in the pipe cold box. They may for example comprise at least 50%, 60%, 70% or 80% of the length of the tubing forming the piping system. At the construction site of the respective air separation plant, the cold boxes are connected to one another and thereby a pipe system is simultaneously established. It is particularly advantageous if the line cold box also contains a subcooler or an ultra-low temperature counter-flow heat exchanger provided in the air separation plant, which can be arranged in a particularly advantageous manner together with the line system.

In the context of the present invention, it can be provided in particular that the first chassis liquid is first conducted through a corresponding filtered counterflow heat exchanger, whether or not it is arranged in a further cold box, and then that this liquid is fed into the fourth separation unit at the first feed position. It can furthermore be provided that the liquid material stream is withdrawn from the first separation unit, guided through the ultra-low temperature counter-current heat exchanger and fed into the fourth separation unit at the second feed position, in the vicinity, preferably directly below the feed position of the liquid inlet stream into the first separation unit. The second feed point into the fourth separation unit is advantageously above the first feed point into the fourth separation unit and is advantageously separated from the latter by at least one separation section.

In particular, in the context of the present invention, a liquid air product may be withdrawn from a distillation column system, raised in pressure in the liquid state, converted to a gaseous or supercritical state by heating, and discharged from an air separation plant. The invention can therefore be used in particular in connection with the so-called internal compression of air products. For a detailed description of the inner compression method reference is made to the cited prior art.

In the context of the present invention, other streams may be withdrawn from the distillation column system and provided as air products. Thus, in particular a gaseous stream can be withdrawn from the fourth separation unit, guided through the ultra-low temperature counter-current heat exchanger and output from the distillation column system as so-called impure nitrogen. The point of withdrawal from the fourth separation unit is advantageously located above the second feeding point into the fourth separation unit. Furthermore, in the context of the present invention, it is also possible for a liquid material stream to be withdrawn in the upper region of the fourth separation unit and to be provided as liquid nitrogen product. In addition, a gaseous nitrogen-rich stream can also be withdrawn in the upper region of the fourth separation unit, conducted through the ultra-low temperature reverse flow heat exchanger, and provided as a corresponding low pressure nitrogen product.

The invention also relates to an air separation plant having a distillation column system comprising a first separation unit, a second separation unit, a third separation unit and a fourth separation unit as described in the respective independent claims.

The air separation plant according to the invention, which is advantageously used for carrying out a process, as explained before, benefits in the same way from the advantages of the process according to the invention in its illustrated embodiment. Therefore, explicit reference is made to the above explanations.

Drawings

FIG. 1 is a partial schematic view of a distillation column system of an air separation plant according to one embodiment of the present invention.

Detailed Description

FIG. 1 shows a simplified partial view of a distillation column system of an air separation plant adapted for operation in accordance with an embodiment of the present invention. The distillation column system shown in figure 1 is generally designated 100. This distillation column system is provided in air separation plant 200, which is only slightly outlined here.

The components of distillation column system 100 shown in fig. 1 include a first separation unit 110, a second separation unit 120, a third separation unit 130, and a fourth separation unit 140, a main condenser 150, an ultra-low temperature counter-current heat exchanger 160, a transfer pump 170, an internal compression pump 180, and an overhead condenser 190.

The first separation unit 110 corresponds to a high pressure column of a conventional air separation plant. The first separation unit operates at a corresponding pressure level, referred to herein as a "first pressure level". The second separation unit 120 and the fourth separation unit 140 correspond to the first section and the second section of the low pressure column of a conventional air separation plant. They all operate at a corresponding common pressure level, referred to herein as the "second pressure level". The third separation unit 130 is an argon discharge column. It is also operated at the second pressure level.

In the distillation column system 100 shown in fig. 1, the first separation unit 110 and the second separation unit 120 are connected in a heat exchange manner by a main condenser 150, as will be explained further below. The first separating element 110 and the second separating element 120 are in particular also arranged within a common column housing and, as described above, are superimposed one on top of the other, in particular directly on top of the other. The overhead condenser 190 is disposed at an upper end of the third separation unit 130. In the alternative shown here, the third separating unit 130 is open in the lower region relative to the upper region of the second separating unit 120. It is also possible to connect the third separation unit 130 to the second separation unit 120 through a pipe extending between an upper region of the second separation unit 120 and a lower region of the third separation unit 130. This case is not separately plotted.

For further description of air separation plants, part of which may be distillation column system 110, see the relevant technical literature, for example(see above) the book, in particular section 2.2.5 and FIG. 2.3A. In such an air separation plant, in particular a gaseous inlet stream 1 and a liquefied inlet stream 2 may be provided. In this connection, in particular, main air compressors, purification and purification devices, turbines, pressure reducing valves and main heat exchangers of known type can be used.

Feed streams 1 and 2 are fed into first separation unit 110 at feed locations 111 and 112, respectively. In the first separation unit 110, an oxygen-rich and nitrogen-lean, argon-containing chassis liquid and a nitrogen-rich and oxygen-lean top gas are formed at a first pressure level. The chassis liquid is withdrawn from first separation unit 110 as stream 3. Overhead gas is withdrawn from first separation unit 110 as stream 4. Liquid in the form of stream 5 is output from the first separation unit 110 directly below the feed location 112 of the inlet stream 2.

Stream 3 is directed through ultra-low temperature counter-current heat exchanger 160 and is partially fed as stream 31 into fourth separation unit 140 at feed position 141. Another portion is transferred as stream 32 to the evaporation chamber of the overhead condenser 190. The liquid stream 33 and the gaseous stream 34 are withdrawn from the evaporation chamber of the overhead condenser 190 and likewise fed into the fourth separation unit 140, and in particular at different heights. Likewise, stream 4 is divided into two streams 41 and 42. The first split stream 41 is partially or completely liquefied in the main condenser 150. The first portion 411 of the first split stream 41 is returned to the first separation unit 110 at feed position 113 as reflux. The second portion 412 of the first split stream 41 is directed through the ultra-low temperature counter-flow heat exchanger 160 and passed to the fourth separation unit 140 as a reflux. A split stream 42 is output from distillation column system 100 as a gaseous compressed nitrogen product. Stream 5 is directed through the ultra-low temperature counter-flow heat exchanger 160 and is fed into the fourth separation unit 140 at feed position 142.

In the second separation unit 120, an oxygen-rich bottom liquid and an argon-rich top gas are formed. The chassis liquid is withdrawn from the second separation unit 120 in stream 6. In the internal compression pump 180, the first partial stream 61 of the feed stream 6 is increased in pressure in the liquid state, converted by heating into the gaseous or supercritical state (not separately shown in fig. 1) and discharged as an internally compressed oxygen product. After being partially directed through the ultra-low temperature counter-current heat exchanger 160 and correspondingly tempered, the second split stream 62 of stream 6 is provided as a liquid oxygen product.

The top gas portion of the second separation unit 120 rises into the third separation unit 130, which is arranged above the second separation unit 120 and opens in the lower region in particular in a manner free from a cross-sectional constriction towards the second separation unit 120. Another portion of the overhead gas is withdrawn as stream 7. Stream 7 is fed to the lower region of fourth separation unit 140 at feed position 143.

In the third separation unit 130, an overhead gas is formed that contains at least a substantial portion of the argon previously contained in the feed gas supplied to the distillation column system 100. The overhead gas is withdrawn from the third separation unit 130 as stream 8. The liquid trickled from the third separation unit 130, which is depleted in argon or (substantially) free of argon in this way, directly arrives again at the second separation unit 120. Therefore, argon discharge is performed in the third separation unit 130.

A bottom liquid and a top gas are formed in the fourth separation unit 140. The bottom liquid is withdrawn from the fourth separation unit 140 in the form of stream 9 and is returned as reflux to the second separation unit 120 by means of the transfer pump 170 and is fed here into the second separation unit 120 at the feed point 114. Stream 10, the so-called impure nitrogen, is withdrawn from the fourth separation unit, directed through an ultra-low temperature counter-current heat exchanger 160, and output from distillation column system 100. The same applies to the nitrogen-rich stream 11 provided as a gaseous low pressure nitrogen product. A nitrogen-rich liquid is withdrawn from the liquid rejection device at the top of the fourth separation unit 140 as stream 12 and provided as a liquid nitrogen product. If no gaseous low pressure nitrogen product is required, the corresponding separation section can be omitted in the fourth separation unit 14 and all of the top gas withdrawn as impure nitrogen equivalent to stream 10.

As shown here, but not necessary for the present invention, a first separation unit 110, a second separation unit 120 and a third separation unit 130 on the one hand and a fourth separation unit 140 on the other hand are provided in the cold box a or B and are connected to each other by means of pipes or conduits, here generally indicated at 20, and/or to other equipment such as an ultra-low temperature counter-current heat exchanger 160 and a main heat exchanger not shown in the figures. The pipe extends vertically at least in sections. At least a part of such a conduit 20 may be arranged in one additional cold box C independently of the two cold boxes a and B in which the first, second and third separation units 110, 120, 130 on the one hand and the fourth separation unit 140 on the other hand are arranged. This additional cold box C for the piping may in particular also contain a subcooler 160.