AIR SEPARATION UNIT AND AIR SEPARATION METHOD

Abstract

The method for reducing or removing non-volatile impurities in a high-purity oxygen liquid comprises: an oxygen vaporization step for vaporizing a high-purity oxygen liquid obtained from a high-purity oxygen rectification column in an air separation unit for producing the high-purity oxygen liquid; and an oxygen recondensing step for recondensing oxygen gas vaporized in the oxygen vaporization step. This method may also comprise a high-purity oxygen liquid extraction step for extracting a condensate obtained in the oxygen recondensing step.

Claims

1. A method for reducing or removing non-volatile impurities in a high-purity oxygen liquid, the method comprising: vaporizing a high-purity oxygen liquid obtained from a high-purity oxygen rectification column in an air separation unit for producing the high-purity oxygen liquid; and recondensing oxygen gas vaporized in the step of vaporizing the high-purity oxygen liquid.

2. The method according to claim 1, wherein the step of recondensing oxygen gas comprises introducing the vaporized oxygen gas below an oxygen mist separator, and extracting a condensate from above the oxygen mist separator.

3. An air separation unit comprising: a nitrogen rectification column having a first nitrogen rectifying portion in which high-boiling-point components are concentrated, and a second nitrogen rectifying portion in which low-boiling-point components are concentrated; a high-purity oxygen rectification column into which an oxygen-containing liquid drawn from the first nitrogen rectifying portion is introduced; a liquid feed pump for feeding an oxygen-rich liquid collected in a bottom of the second nitrogen rectification column to a column top of the first nitrogen rectifying portion; an oxygen vaporizer which is arranged in a lower portion of the high-purity oxygen rectification column and serves to generate a vapour stream of oxygen gas; and an oxygen recondenser into which a portion of the oxygen gas generated in the oxygen vaporizer is introduced, in order to condense this oxygen gas.

4. The air separation unit according to claim 3, further comprising an oxygen mist separator on a primary side of the oxygen recondenser, wherein a portion of the oxygen gas generated in the oxygen vaporizer is introduced below the oxygen mist separator.

5. An air separation unit comprising: a nitrogen rectification column; a high-purity oxygen rectification column having a first oxygen rectifying portion in which high-boiling-point components are concentrated, and a second oxygen rectifying portion in which low-boiling-point components are concentrated; a liquid feed pump for feeding an oxygen-rich liquid collected in a bottom of the first oxygen rectifying portion to a column top of the second oxygen rectifying portion; an oxygen vaporizer which is arranged in a lower portion of the second oxygen rectifying portion and serves to generate a vapour stream of oxygen gas; and an oxygen recondenser into which a portion of the oxygen gas generated in the oxygen vaporizer is introduced, in order to condense this oxygen gas.

6. The air separation unit according to claim 5, further comprising an oxygen mist separator on a primary side of the oxygen recondenser, wherein a portion of the oxygen gas generated in the oxygen vaporizer is introduced below the oxygen mist separator.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0074] Other features and advantages of the invention will be further disclosed in the description that follows, and in several embodiments provided as non-limiting examples in reference to the appended schematic drawings, in which:

[0075] FIG. 1 illustrates an air separation unit according to embodiment 1.

[0076] FIG. 2 illustrates an air separation unit according to embodiment 2.

[0077] FIG. 3 illustrates an air separation unit according to embodiment 3.

[0078] FIG. 4 illustrates an air separation unit according to embodiment 4.

DETAILED DESCRIPTION OF THE INVENTION

[0079] Several embodiments of the present disclosure will be described below. The embodiments described below are given as an example of the present disclosure. The present disclosure is in no way limited by the following embodiments, and also includes a number of variant modes which are implemented within a scope that does not alter the essential point of the present disclosure. It should be noted that not all the constituents described below are necessarily essential to the present disclosure. Upstream and downstream are based on a flow direction of a gas stream.

Embodiment 1

[0080] An air separation unit A1 according to embodiment 1 will be described with the aid of FIG. 1.

[0081] The air separation unit A1 comprises: a nitrogen rectification column 2 having a first nitrogen rectifying portion 21 in which high-boiling-point components are concentrated, and a second nitrogen rectifying portion 22 in which low-boiling-point components are concentrated; and a high-purity oxygen rectification column 5. The first nitrogen rectifying portion 21 and the second nitrogen rectifying portion 22 are separated because of constraints such as height constraints, and a liquid feed pump 8 is provided in order to feed an oxygen-rich liquid collected in a bottom 221 of the second nitrogen rectifying portion 22 to a column top 213 of the first nitrogen rectifying portion 21.

[0082] The air separation unit A1 comprises: a main heat exchanger 1 for subjecting feed air to heat exchange, an expander-compressor 9, and an oxygen recondenser 7.

[0083] The feed air that has passed through the main heat exchanger 1 is introduced into the first nitrogen rectifying portion 21. The feed air is introduced into a lower rectifying portion in this embodiment. A feed air pipeline L1 passes the feed air through the main heat exchanger 1 and introduces the feed air into the lower rectifying portion of the first nitrogen rectifying portion 21.

[0084] A gas (vaporized gas) drawn from the column top 213 of the first nitrogen rectifying portion 21 is introduced into the second nitrogen rectifying portion 22. The gas is introduced into a gas phase below a rectifying portion 222 or in the bottom 221 in this embodiment. A pipeline L213 feeds the gas (vaporized gas) drawn from the column top 213 of the first nitrogen rectifying portion 2 to the second nitrogen rectifying portion 22.

[0085] The gas (vaporized gas) drawn from a column top 223 of the second nitrogen rectifying portion 22 is introduced into first and second condensers 3, 4 which condense (cool) this gas and return it to the column top 223. The second condenser 4 is arranged above the first condenser 3 in this embodiment. A pipeline L211a feeds an oxygen-rich liquid drawn from a bottom 211 of the first nitrogen rectifying portion 21 to be used as cold heat in the second condenser 4. A pipeline is also provided for feeding the oxygen-rich liquid from the second condenser 4 to the first condenser 3.

[0086] An expander 92 of the expander-compressor 9 expands a gas drawn from a column top 31 of the first condenser 3, after the gas has passed through a part of the main heat exchanger 1. The expanded gas is passed through the main heat exchanger 1 and treated as waste gas. By way of a waste gas pipeline L31, the gas which is drawn from the column top 31 of the first condenser 3 is passed through a part of the main heat exchanger 1, expanded in the expander 92, and then passed through the main heat exchanger 1, from which it is drawn.

[0087] A compressor 91 of the expander-compressor 9 compresses the gas drawn from a column top 41 of the second condenser 4. The compressed gas passes through a part of the main heat exchanger 1 and is introduced into the gas phase in the bottom 211 of the first nitrogen rectifying portion 21. By way of a recycling pipeline L41, the gas which is drawn from the column top 41 of the second condenser 4 is compressed by the compressor 91, passed through a part of the main heat exchanger 1, and introduced into the first nitrogen rectifying portion 21.

[0088] A nitrogen-rich gas drawn from the column top 223 of the second nitrogen rectifying portion 22 is passed, by way of a nitrogen gas line L223, through the main heat exchanger 1, from which it is drawn.

[0089] An oxygen-containing liquid (including a gaseous form and a liquid form) drawn from an intermediate portion 212 of the first nitrogen rectifying portion 21 is introduced into the high-purity oxygen rectification column 5. A pipeline L212 draws the oxygen-containing liquid from the intermediate portion 212 of the first nitrogen rectifying portion 21 and introduces the liquid into a column top 53 of the high-purity oxygen rectification column 5.

[0090] An oxygen vaporizer 55 for generating a vapour stream of oxygen gas is provided in a lower portion of the oxygen rectifying portion of the high-purity oxygen rectification column 5. A pipeline L211b draws the oxygen-rich liquid from the bottom 211 of the first nitrogen rectifying portion 21 and uses this as cold heat in the oxygen vaporizer 55, after which the oxygen-rich liquid is fed to the second condenser 4 and used as cold heat.

[0091] A portion of the oxygen gas (vapour stream) generated in the oxygen vaporizer 55 is introduced into the oxygen recondenser 7, where the oxygen gas is condensed (reliquefied). A pipeline L522 draws a portion of the oxygen gas (vapour stream) generated in the oxygen vaporizer 55, and introduces the oxygen gas into the oxygen recondenser 7. A pipeline L211b1 which branches from a pipeline L211b feeds the oxygen-rich liquid after usage in the oxygen vaporizer 55 to the oxygen recondenser 7 for use as cold heat, then merges into the waste gas pipeline L31 upstream of the main heat exchanger 1.

[0092] The high-purity oxygen gas from which non-volatile impurities have been separated in the oxygen vaporizer 55 is fed via a pipeline L522 to the oxygen recondenser 7 where it can be recondensed as high-purity oxygen liquid free from non-volatile impurities.

[0093] A pipeline L53 draws the gas from the column top 53 of the high-purity oxygen rectification column 5 and merges into the waste gas pipeline (L31) upstream of the main heat exchanger (1).

[0094] A first extraction pipeline L71 extracts a high-purity oxygen liquid reliquefied in a bottom 71 of the oxygen recondenser 7. The high-purity oxygen liquid extracted by the first extraction pipeline L71 may be pressurized to a predetermined pressure by a pressurization apparatus and then fed to a point of demand. The high-purity oxygen liquid extracted by the first extraction pipeline L71 may be passed through the main heat exchanger 1 (vaporized) to form oxygen gas which is then fed to a point of demand.

Embodiment 2

[0095] An air separation unit A2 according to embodiment 2 will be described with the aid of FIG. 2. The air separation unit A2 of embodiment 2 mainly differs from the air separation unit A1 of embodiment 1 in that the air separation unit A2 comprises an oxygen mist separator. Components which are the same as those of embodiment 1 will not be described or will only be briefly described.

[0096] An oil mist separator 75 is provided on a primary side (in a lower portion) of the oxygen recondenser 7. The pipeline L522 introduces a portion of the oxygen gas (vapour stream) generated in the oxygen vaporizer 55 to below the oxygen mist separator 75.

[0097] A second extraction pipeline L72 extracts the high-purity oxygen liquid from above the oxygen mist separator 75 in the oxygen recondenser 7. A pipeline L711 draws the high-purity oxygen liquid collected in the bottom 71 of the oxygen recondenser 7 and introduces the liquid to above the oxygen vaporizer 55 in the high-purity oxygen rectification column 5. The high-purity oxygen liquid extracted by the second extraction pipeline L72 may be pressurized to a predetermined pressure by a pressurization apparatus and then fed to a point of demand. The high-purity oxygen liquid extracted by the first extraction pipeline L72 may be passed through the main heat exchanger 1 (vaporized) to form oxygen gas which is then fed to a point of demand.

[0098] The oxygen mist separator 75 may employ, for example: a water(-drop) separator, a mist eliminator, structured packing, or random packing, etc. A liquid fraction and impurities in the liquid fraction are removed from the oxygen gas in the vapour stream. When the vapour stream is introduced below the oxygen mist separator 75 and the vapour stream rises to pass through the oxygen mist separator 75, the high-concentration oxygen liquid in the bottom 71 rises together with the vapour stream but is blocked by the oxygen mist separator 75 and travels no further.

Embodiment 3

[0099] An air separation unit B1 according to embodiment 3 will be described with the aid of FIG. 3. The air separation unit B1 according to embodiment 3 comprises: a nitrogen rectification column 200; and a high-purity oxygen rectification column 5 having a first oxygen rectifying portion 51 in which high-boiling-point components are concentrated, and a second oxygen rectifying portion 52 in which low-boiling-point components are concentrated. The first oxygen rectifying portion 51 and the second oxygen rectifying portion 52 are separated because of constraints such as height constraints, and a liquid feed pump 81 is provided in order to feed an oxygen-rich liquid collected in a bottom 511 of the first oxygen rectifying portion 51 to a column top 523 of the second oxygen rectifying portion 52.

[0100] The air separation unit B1 comprises: a main heat exchanger 1 for subjecting feed air to heat exchange, an expander-compressor 9, and an oxygen recondenser 7.

[0101] The feed air that has passed through the main heat exchanger 1 is introduced into the nitrogen rectification column 200 via a pipe L1.

[0102] An oxygen-rich liquid drawn from a bottom 201 of the nitrogen rectification column 200 is fed to a second condenser 4 via a pipeline L201a to be used as cold heat. Furthermore, the oxygen-rich liquid is fed from the second condenser 4 to a first condenser 3.

[0103] A gas (vaporized gas) drawn from a column top 203 of the nitrogen rectification column 200 is introduced into the first and second condensers 3, 4 which condense (cool) this gas and return it to the column top 203.

[0104] An expander 92 of the expander-compressor 9 expands a gas drawn from a column top 31 of the first condenser 3 via a waste gas pipeline L31, after the gas has passed through a part of the main heat exchanger 1. The expanded gas is passed through the main heat exchanger 1 via the waste gas pipeline L31 and treated as waste gas.

[0105] A compressor 91 of the expander-compressor 9 compresses the gas drawn from a column top 41 of the second condenser 4 via a recycling pipeline L41. The compressed gas passes through a part of the main heat exchanger 1 via the recycling pipeline L41 and is introduced into the gas phase in the bottom 201 of the nitrogen rectification column 200.

[0106] A nitrogen-rich gas drawn from the column top 23 of the nitrogen rectification column 2 is passed, by way of a nitrogen gas line L203, through the main heat exchanger 1, from which it is drawn.

[0107] An oxygen-containing liquid (including a gaseous form and a liquid form) is introduced into a column top 513 of the first oxygen rectifying portion 51 from an intermediate portion 202 of the nitrogen rectification column 200 via a pipe L202. A pipeline L513 merges a gas, which is drawn from the column top 513 of the first oxygen rectifying portion 51, into the waste gas pipeline L31 upstream of the main heat exchanger 1.

[0108] An oxygen-rich liquid is drawn from the bottom 511 of the first oxygen rectifying portion 51 via a pipe L511 and introduced into the column top 523 of the second oxygen rectifying portion 52 by using a liquid feed pump 81. A pipeline L523 feeds a gas from the column top 523 of the second oxygen rectifying portion 52 to a gas phase in the bottom 511 of the first oxygen rectifying portion 51.

[0109] A pipeline L201b introduces an oxygen-rich liquid drawn from the bottom 201 of the nitrogen rectification column 200 into an oxygen vaporizer 55 to be used as cold heat, and then feeds the liquid to the second condenser 4. A pipeline L201b1 which branches from the pipeline L201b feeds the oxygen-rich liquid after usage in the oxygen vaporizer 55 to the oxygen recondenser 7 for use as cold heat, then merges into the waste gas pipeline L31 upstream of the main heat exchanger 1.

[0110] The oxygen vaporizer 55 for generating a vapour stream of oxygen gas is provided in a lower portion of the oxygen rectifying portion of the second oxygen rectifying portion 52.

[0111] A portion of the oxygen gas (vapour stream) generated in the oxygen vaporizer 55 is introduced into the oxygen recondenser 7 via a pipeline L522, where the oxygen gas is condensed (reliquefied).

[0112] A pressurization apparatus (10) pressurizes the high-purity oxygen liquid drawn from a bottom 71 of the oxygen recondenser 7 via a pipe L712.

[0113] A third extraction pipe L101 extracts a pressurized high-purity oxygen liquid from the bottom of the pressurization apparatus 10. The high-purity oxygen liquid extracted by the third extraction pipeline L101 may be passed through the main heat exchanger 1 (vaporized) to form oxygen gas which is then fed to a point of demand.

[0114] A pipeline L102 introduces oxygen gas drawn from the pressurization apparatus 10 to above the oxygen vaporizer 55 in the oxygen vaporizer 55 of the second oxygen rectifying portion 52.

Embodiment 4

[0115] An air separation unit B2 according to embodiment 4 will be described with the aid of FIG. 4. The air separation unit B2 of embodiment 4 mainly differs from the air separation unit B1 of embodiment 3 in that the air separation unit A2 comprises an oxygen mist separator. Components which are the same as those of embodiment 3 will not be described or will only be briefly described.

[0116] An oil mist separator 75 is provided on a primary side (in a lower portion) of the oxygen recondenser 7. The pipeline L522 introduces a portion of the oxygen gas (vapour stream) generated in the oxygen vaporizer 55 to below the oxygen mist separator 75.

[0117] A pipeline L721 extracts the high-purity oxygen liquid from above the oxygen mist separator 75 in the oxygen recondenser 7. A pipeline L711 draws the high-purity oxygen liquid collected in the bottom 71 of the oxygen recondenser 7 and introduces the liquid to above the oxygen vaporizer 55 in the high-purity oxygen rectification column 5. The high-purity oxygen liquid extracted by the pipeline L721 is fed to the pressurization apparatus 10.

[0118] The pressurization apparatus 10 pressurizes the high-purity oxygen liquid to a predetermined pressure. A third extraction pipe L101 extracts a pressurized high-purity oxygen liquid from the bottom of the pressurization apparatus 10. The high-purity oxygen liquid extracted by the third extraction pipeline L101 may be passed through the main heat exchanger 1 (vaporized) to form oxygen gas which is then fed to a point of demand.

[0119] A pipeline L102 introduces oxygen gas drawn from the pressurization apparatus 10 to above the oxygen vaporizer 55 in the second oxygen rectifying portion 52.

Embodiment 1, Example in FIG. 1

[0120] Feed air is supplied to a warm end of the main heat exchanger 1 at 10.31 barA, a temperature of 55 C., and a flow rate of 1050 Nm.sup.3/h, cooled to 164.2 C., and then supplied to the first nitrogen rectifying portion 21 of the nitrogen rectification column 2. Nitrogen gas is drawn from the column top 223 of the second nitrogen rectifying portion 22 at 532 Nm.sup.3/h, warmed in the main heat exchanger 1, and then drawn out.

[0121] A rich liquid comprising 39% oxygen is drawn from the bottom 211 of the first nitrogen rectifying portion 21 at 802 Nm.sup.3/h, 137 Nm.sup.3/h thereof is supplied to the second nitrogen condenser 4, another 655 Nm.sup.3/h thereof is cooled to 175.4 C. in the oxygen vaporizer 55, after which 644 Nm.sup.3/h of that is supplied to the second nitrogen condenser 4 while the remaining 11 Nm.sup.3/h is supplied as a refrigerant to the oxygen recondenser 7, and after warming, is mixed with waste gas supplied from the expander 92 (expansion turbine), then warmed in the main heat exchanger 1 and discharged.

[0122] Recycled air is generated in the second nitrogen condenser 4 at 6.2 barA and 390 Nm.sup.3/h, the pressure is boosted to 10.2 barA in the compressor 91, after which the recycled air is cooled in the main heat exchanger 1 then recycled to the first nitrogen rectifying portion 21.

[0123] Waste gas is further generated in the first nitrogen condenser 3 at 4.7 barA and 399 Nm.sup.3/h, warmed to 141 C. in the main heat exchanger 1, and then cooled while simultaneously being expanded in the expander 92 (expansion turbine), once again warmed in the main heat exchanger 1, and then discharged.

[0124] In order to produce high-purity oxygen, an oxygen-containing liquid comprising 18% oxygen is drawn from the first nitrogen rectifying portion 21 at 106 Nm.sup.3/h, decompressed to 1.5 barA, and then supplied to the column top 53 of the high-purity oxygen rectification column 5. Waste gas is drawn from the column top 53 at 97 Nm.sup.3/h, mixed with the waste gas supplied from the expander 92 (expansion turbine), then warmed in the main heat exchanger 1 and discharged.

[0125] Oxygen gas is drawn at 9 Nm.sup.3/h from above (52) the oxygen vaporizer 55 in the high-purity oxygen rectification column 5 and liquefied in the oxygen recondenser 7, and a high-purity oxygen liquid is collected in the bottom 71.

[0126] The nitrogen rectification column 2 is divided into two parts above and below, and the liquid feed pump 8 (reflux liquid pump) is arranged intermediately between the two parts. In this example, if the number of theoretical stages in the nitrogen rectification column 2 is 68, and the point of division is an intermediate point of 34 in the number of theoretical stages, then the amount of reflux liquid treated by the liquid feed pump 8 is 998 Nm.sup.3/h. For the number of theoretical stages, the stage at the bottommost point of the rectification column is taken as the first stage, and the stage at the topmost point is taken as the 68th stage. In this case, the point at which the oxygen-containing liquid is drawn is the point at the 15th theoretical stage, and the amount of reflux liquid supplied at this point is 933 Nm.sup.3/h.

[0127] When metal impurities (non-volatile impurities) corresponding to 1 ppb are mixed with the reflux liquid from the liquid feed pump 8, the amount of metal impurities in the oxygen-containing liquid is as follows.

1 [ppb]998 [Nm.sup.3/h]933 [Nm.sup.3/h]=1.07 [ppb]

[0128] Additionally, the oxygen-containing liquid is introduced into the high-purity oxygen rectification column 5 at 106 Nm.sup.3/h, and oxygen corresponding to 9 Nm.sup.3/h is concentrated in the bottom 51. The following metal impurities are contained in terms of the oxygen liquid.

1.07 [ppb]106 [Nm.sup.3/h]9 [Nm.sup.3/h]=12.6 [ppb]

[0129] In terms of oxygen gas in this embodiment 1, as shown in FIG. 1, metal impurities are not contained in the oxygen gas when oxygen is drawn from the bottom 51 of the high-purity oxygen rectification column 5 because these metal impurities are non-volatile, and by condensing the oxygen gas in the oxygen recondenser 7, it is possible to obtain a high-purity oxygen liquid free from metal impurities.

[0130] The liquid oxygen can be pressurized by externally input heat, without using a pump or a compressor, and is therefore suitable for supplying high-purity oxygen. In this method, the metal impurities are accumulated in the lower portion of the high-purity oxygen rectification column, but since there is sufficient space in the bottom of the high-purity oxygen rectification column, there are no problems such as obstruction of the oxygen flow path within the heat exchanger, even if the metal impurities build up over the period of operation of the oxygen rectification column, and the impurities can also be discharged by regularly purging with liquid oxygen.

Embodiment 2, Example in FIG. 2

[0131] The oxygen mist separator 75 is arranged in a lower portion of the oxygen recondenser 7. When the piping for drawing gas from above (52) the oxygen vaporizer 55 in the high-purity oxygen rectification column 5 is designed, there is a possibility of there being liquid drops around a drawing pipe inlet. These liquid drops include those which have fallen after being supplied to the high-purity oxygen rectification column 5 as the reflux liquid, and also those which result from the high-purity oxygen liquid (including metal impurities) collected in the bottom of the high-purity oxygen rectification column 5 being swept up so as to be entrained with oxygen gas supplied from the oxygen vaporizer 55, and these liquid drops may therefore contain non-volatile impurities.

[0132] Accordingly, the height is set at a sufficient level to prevent splashing and entrainment by taking account of the physical properties of the liquid drops and the flow rate of oxygen gas so that these liquid drops (microspray) do not enter the oxygen recondenser 7 while entrained with the oxygen gas which is drawn. However, the interior of the oxygen recondenser 7 is decompressed along with drawing of the high-purity oxygen liquid from the oxygen recondenser 7 and condensation of the oxygen gas, which produces a large difference in pressure between the high-purity oxygen rectification column 5 and the oxygen recondenser 7 (internal pressure of oxygen recondenser 7 is greater than internal pressure of oxygen rectification column 5), and the oxygen gas flows through the piping at a high rate as a result, so liquid drops may be carried into the oxygen recondenser 7. The mist separator 75 enables liquid drops carried into the oxygen recondenser 7 in this way to be separated from the oxygen gas, and oxygen gas free from liquid drops can be condensed in the oxygen recondenser 7.

Embodiment 3, Example in FIG. 3

[0133] The high-purity oxygen rectification column 5 is divided into two parts above and below. The liquid feed pump 81 (reflux liquid pump) is arranged at an intermediate portion. If the number of theoretical stages in the high-purity oxygen rectification column 5 is 59, and the point of division is an intermediate point of 30 in the number of theoretical stages, then the amount of reflux liquid treated by the liquid feed pump 81 is 69 Nm.sup.3/h. When metal impurities corresponding to 1 ppb are mixed with the reflux liquid from the liquid feed pump 81, the following metal impurities are contained in terms of the oxygen liquid which may be drawn from the high-purity oxygen rectification column 5.

1 [ppb]69 [Nm.sup.3/h]9 [Nm.sup.3/h]=7.7 [ppb]

[0134] In terms of oxygen gas in this embodiment 3, as shown in FIG. 3, metal impurities are not contained in the oxygen gas vaporized by the oxygen vaporizer 55 when oxygen is drawn from the bottom 521 of the second oxygen rectifying portion 52 because these metal impurities are non-volatile, and by feeding the oxygen gas to the oxygen recondenser 7 to be condensed, it is possible to obtain a high-purity oxygen liquid free from metal impurities.

Embodiment 4, Example in FIG. 4

[0135] The oxygen mist separator 75 is arranged in a lower portion of the oxygen recondenser 7. The effects are the same as those of embodiment 2.

Other Embodiments

[0136] Although not explicitly stated, pressure regulators and flow rate controllers, etc. may be provided in each pipeline in order to regulate pressure and regulate flow.

[0137] Although not explicitly stated, control valves and gate valves, etc. may be provided in each line.

[0138] Although not explicitly stated, pressure regulators and temperature measurement devices, etc. may be provided in each column in order to regulate pressure and regulate temperature.

[0139] While the invention has been described in conjunction with specific embodiments thereof, it is evident that many alternatives, modifications, and variations will be apparent to those skilled in the art in light of the foregoing description. Accordingly, it is intended to embrace all such alternatives, modifications, and variations as fall within the spirit and broad scope of the appended claims. The present invention may suitably comprise, consist or consist essentially of the elements disclosed and may be practiced in the absence of an element not disclosed. Furthermore, if there is language referring to order, such as first and second, it should be understood in an exemplary sense and not in a limiting sense. For example, it can be recognized by those skilled in the art that certain steps can be combined into a single step.

[0140] The singular forms a, an and the include plural referents, unless the context clearly dictates otherwise.

[0141] Comprising in a claim is an open transitional term which means the subsequently identified claim elements are a nonexclusive listing (i.e., anything else may be additionally included and remain within the scope of comprising). Comprising as used herein may be replaced by the more limited transitional terms consisting essentially of and consisting of unless otherwise indicated herein.

[0142] Providing in a claim is defined to mean furnishing, supplying, making available, or preparing something. The step may be performed by any actor in the absence of express language in the claim to the contrary.

[0143] Optional or optionally means that the subsequently described event or circumstances may or may not occur. The description includes instances where the event or circumstance occurs and instances where it does not occur.

[0144] Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such a range is expressed, it is to be understood that another embodiment is from the one particular value and/or to the other particular value, along with all combinations within said range.

KEY TO SYMBOLS

[0145] Main heat exchanger [0146] Nitrogen rectification column [0147] First condenser [0148] Second condenser [0149] High-purity oxygen rectification column [0150] 55 Oxygen vaporizer [0151] Oxygen recondenser [0152] Liquid feed pump [0153] Expander-compressor