JPS6333066B2 - - Google Patents
Info
- Publication number
- JPS6333066B2 JPS6333066B2 JP55136111A JP13611180A JPS6333066B2 JP S6333066 B2 JPS6333066 B2 JP S6333066B2 JP 55136111 A JP55136111 A JP 55136111A JP 13611180 A JP13611180 A JP 13611180A JP S6333066 B2 JPS6333066 B2 JP S6333066B2
- Authority
- JP
- Japan
- Prior art keywords
- argon
- column
- nitrogen
- crude argon
- crude
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 164
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 103
- 229910052786 argon Inorganic materials 0.000 claims description 82
- 229910052757 nitrogen Inorganic materials 0.000 claims description 51
- 239000007788 liquid Substances 0.000 claims description 16
- 238000004519 manufacturing process Methods 0.000 claims description 8
- 238000000034 method Methods 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 5
- 239000007789 gas Substances 0.000 description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 11
- 239000001301 oxygen Substances 0.000 description 11
- 229910052760 oxygen Inorganic materials 0.000 description 11
- 230000000630 rising effect Effects 0.000 description 4
- 238000007711 solidification Methods 0.000 description 4
- 230000008023 solidification Effects 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- PWKWDCOTNGQLID-UHFFFAOYSA-N [N].[Ar] Chemical compound [N].[Ar] PWKWDCOTNGQLID-UHFFFAOYSA-N 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04436—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system
- F25J3/04448—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system in a double column flowsheet with an intermediate pressure column
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
- F25J3/04733—Producing pure argon, e.g. recovered from a crude argon column using a hybrid system, e.g. using adsorption, permeation or catalytic reaction
- F25J3/04739—Producing pure argon, e.g. recovered from a crude argon column using a hybrid system, e.g. using adsorption, permeation or catalytic reaction in combination with an auxiliary pure argon column
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/82—Processes or apparatus using other separation and/or other processing means using a reactor with combustion or catalytic reaction
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
【発明の詳細な説明】
この発明は空気液化精留法によつて空気分離装
置よりアルゴンを採取する装置に関し、詳しくは
空気分離装置から粗アルゴン塔に供給されるフイ
ードガス中の窒素分が増加しても粗アルゴン塔を
安定に運転できるようにし、アルゴンの回収率を
向上せしめるようにしたものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an apparatus for extracting argon from an air separation apparatus using an air liquefaction rectification method. The crude argon column can be operated stably even when the argon is used, and the recovery rate of argon can be improved.
空気液化精留法によつてアルゴンを採取するに
は原料空気を圧縮冷却した後、複式精留塔におい
て酸素と窒素に分離し、アルゴン含有量の高い酸
素（以下、フイードガスと言う）を抽出して精留
および精製するのが普通である。第１図を参照し
てフイードガスより高純アルゴンを分離精製する
一般的な実施例を説明する。複式精留塔１の低圧
塔２中部よりアルゴン８〜15vol％、窒素100〜
1000ppm、残り酸素の組成をもつたフイードガス
が管３より粗アルゴン塔４下部に吸引される。こ
のフイードガスは粗アルゴン塔４内を上昇し、複
式精留塔１の中圧塔５より管６、弁７を経て粗ア
ルゴン塔４の上部に設けられた凝縮器８に供給さ
れる還流用冷却源である液体空気によつて冷却液
化流下して精留され、その結果、粗アルゴン塔４
の上部より管９を介して粗アルゴン（アルゴン95
〜98vol％、酸素１〜2vol％、窒素１〜2vol％）
が導出されるとともに底部の管１０より液体酸素
が導出され低圧塔２へ返送される。 To collect argon using the air liquefaction rectification method, raw air is compressed and cooled, separated into oxygen and nitrogen in a double rectification column, and oxygen with a high argon content (hereinafter referred to as feed gas) is extracted. It is common practice to rectify and purify the product. A general embodiment for separating and purifying high purity argon from feed gas will be described with reference to FIG. Argon 8-15vol%, nitrogen 100-100vol% from the middle of low pressure column 2 of double rectification column 1
Feed gas having a composition of 1000 ppm and residual oxygen is drawn into the lower part of the crude argon column 4 through pipe 3. This feed gas rises in the crude argon column 4, passes through the pipe 6 and valve 7 from the medium pressure column 5 of the double rectification column 1, and is supplied to the condenser 8 provided at the upper part of the crude argon column 4 for reflux cooling. The source liquid air cools the liquefied stream and rectifies it, resulting in a crude argon column 4.
Coarse argon (argon 95
~98vol%, oxygen 1-2vol%, nitrogen 1-2vol%)
At the same time, liquid oxygen is led out from the bottom pipe 10 and returned to the low pressure column 2.
管９より導出された粗アルゴンは熱交換器１１
により熱交換されて昇温され、ブロワ１２で加圧
され、水素供給源１３より水素を加えられて脱酸
反応器１４で脱酸素され、水分離器１５、乾燥器
１６で脱酸反応の結果、生成した水分が除去さ
れ、熱交換器１１で熱交換されて冷却され、高純
アルゴン塔１７で精留され、高純アルゴンが得ら
れる。 The crude argon led out from the tube 9 is transferred to the heat exchanger 11
The hydrogen is heated by heat exchange and heated up, pressurized by a blower 12, hydrogen is added from a hydrogen supply source 13, deoxidized in a deoxidizing reactor 14, and the result of a deoxidizing reaction is carried out in a water separator 15 and a dryer 16. The generated moisture is removed, cooled by heat exchange in a heat exchanger 11, and rectified in a high-purity argon column 17 to obtain high-purity argon.
空気液化精留法による空気分離装置によりアル
ゴンを採取するには一般に上述のようにして行わ
れるが、低圧塔２より粗アルゴン塔４に供給され
るフイードガス中のアルゴン含有量は低圧塔２、
中圧塔５の運転状態によつて異なり、低圧塔２に
おいて通常の運転状態では低圧塔２の中下部でア
ルゴン含有量が最大となる。このアルゴン含有量
が最大となる部分のフイードガスを粗アルゴン塔
４へ導入すればアルゴン収率の点から有利である
がこのフイードガスには窒素が多く、これを粗ア
ルゴン塔４へ導入すると粗アルゴン塔４頂部での
粗アルゴン中の窒素が著しく多くなる。従つて凝
縮器８での液体空気との熱交換が困難になり粗ア
ルゴン塔４の運転が不可能となつてしまう。従つ
て、一般には、アルゴンの収率を犠性にして上述
のように窒素の少ない低圧塔５下部よりフイード
ガスの供給を受けて、粗アルゴン塔４の運転が正
常となるようにしているのが実情である。 Argon is generally collected by an air separation device using an air liquefaction rectification method as described above, but the argon content in the feed gas supplied from the low pressure column 2 to the crude argon column 4 is
The argon content varies depending on the operating state of the intermediate pressure column 5, and in the normal operating state of the low pressure column 2, the argon content is maximum in the middle and lower part of the low pressure column 2. It is advantageous in terms of argon yield to introduce the portion of the feed gas with the maximum argon content into the crude argon column 4, but this feed gas contains a lot of nitrogen, and if it is introduced into the crude argon column 4, the crude argon column 4 There is a significant increase in nitrogen in the crude argon at the top. Therefore, heat exchange with liquid air in the condenser 8 becomes difficult, making it impossible to operate the crude argon column 4. Therefore, in general, the crude argon column 4 is operated normally by receiving feed gas from the lower part of the low pressure column 5, which is low in nitrogen, as described above, at the expense of the argon yield. This is the reality.
この発明は上記事情に鑑みてなされたもので、
複式精留塔の低圧塔の中下部からアルゴン含有量
が最大で窒素分の多いフイードガスを供給しても
粗アルゴン塔を安定に運転することができ、アル
ゴンの収率を向上できるアルゴンの製造装置を提
供することを目的とし、粗アルゴン塔上部に窒素
精留塔を設け、この窒素精留塔上部に、中圧塔上
部から液体窒素を還流液として直接導入するよう
に構成したことを特徴とするものである。 This invention was made in view of the above circumstances,
An argon production device that can stably operate the crude argon column and improve the argon yield even when feed gas with the maximum argon content and high nitrogen content is supplied from the middle and lower parts of the low-pressure column of the double rectification column. A nitrogen rectification column is provided at the top of the crude argon column, and liquid nitrogen is directly introduced into the top of the nitrogen rectification column as a reflux liquid from the top of the medium pressure column. It is something to do.
以下、図面を参照してこの発明を説明する。第
２図はこの発明のアルゴン製造装置の一例を示す
フローチヤートであるが、第１図に示す装置と同
一構成部分については同一符号を付してその説明
を省略する。 The present invention will be described below with reference to the drawings. FIG. 2 is a flowchart showing an example of the argon production apparatus of the present invention, and the same components as those of the apparatus shown in FIG.
この発明のアルゴンの製造装置の粗アルゴン塔
４は粗アルゴン塔４の上部の凝縮器８の上部に窒
素精留塔１８として精留段が連続して設けられ、
中圧塔５上部より管１９、弁２０を経て窒素精留
塔１８上部に液化窒素を直接導入するように構成
されている。低圧塔２中下部のアルゴン含有量が
最大となる部分より管３で、アルゴン含有量が最
大で窒素の多いフイードガスが粗アルゴン塔４下
部に供給され、塔内を上昇ガスとして上昇する間
に気液接触して、アルゴン約95〜97vol％、酸素
３〜2vol％、窒素３〜1vol％の粗アルゴンとな
り、管９によつて導出され、以下、前述の従来法
と同様に精製されて高純アルゴンを得る。 The crude argon column 4 of the argon production apparatus of the present invention is provided with a rectification stage continuously provided as a nitrogen rectification column 18 above the condenser 8 in the upper part of the crude argon column 4.
The structure is such that liquefied nitrogen is directly introduced from the upper part of the intermediate pressure column 5 into the upper part of the nitrogen rectification column 18 via a pipe 19 and a valve 20. Feed gas with the highest argon content and nitrogen content is supplied to the lower part of the crude argon column 4 through pipe 3 from the middle and lower part of the low pressure column 2 where the argon content is maximum. Upon contact with the liquid, crude argon containing about 95 to 97 vol% argon, 3 to 2 vol% oxygen, and 3 to 1 vol% nitrogen is produced, which is led out through the tube 9, and then purified in the same manner as in the conventional method described above to obtain high purity. Get argon.
上昇ガスのほとんどは凝縮器８にて液化空気と
熱交換して液化し、粗アルゴン塔４内を還流液と
して流下する。上昇ガスの残部はそのまま窒素精
留塔１８を上昇し、頂部で酸素100〜200ppm、ア
ルゴン１〜3vol％、残窒素の組成の窒素ガスとし
て管２１より抜出される。一方、窒素精留塔１８
の頂部には前記したように高純液化窒素が導入さ
れ窒素精留塔１８内を上昇してくる前記上昇ガス
と気液接触して流下してゆく。粗アルゴン塔４の
塔底からは液体酸素が管１０を通り低圧塔２に返
送される。 Most of the rising gas is liquefied by exchanging heat with liquefied air in the condenser 8, and flows down in the crude argon column 4 as a reflux liquid. The remainder of the rising gas ascends as it is through the nitrogen rectification column 18, and is extracted from the pipe 21 at the top as nitrogen gas having a composition of 100 to 200 ppm oxygen, 1 to 3 vol% argon, and residual nitrogen. On the other hand, nitrogen rectification column 18
As described above, high-purity liquefied nitrogen is introduced into the top of the nitrogen rectification column 18, comes into gas-liquid contact with the rising gas rising in the nitrogen rectification column 18, and flows down. From the bottom of the crude argon column 4, liquid oxygen is returned to the low pressure column 2 through a pipe 10.
窒素精留塔１８には上述の如く液体窒素が直接
導入されるので、窒素精留塔１８内の操作温度が
アルゴンの固化点以下になるが、各棚段でのアル
ゴン―窒素組成比に対応する固化点は第３図に示
すように操作温度よりも低いのでアルゴンの固化
は起らず、安定に窒素精留塔１８を運転すること
ができる。 Since liquid nitrogen is directly introduced into the nitrogen rectification column 18 as described above, the operating temperature within the nitrogen rectification column 18 is below the solidification point of argon, but it corresponds to the argon-nitrogen composition ratio in each tray. Since the solidification point is lower than the operating temperature as shown in FIG. 3, solidification of argon does not occur and the nitrogen rectification column 18 can be operated stably.
なお、窒素精留塔１８に導入する液体窒素の量
は得られる粗アルゴンと同量程度でよいが、この
量を増加してやれば粗アルゴン中の窒素を減らす
ことができる。また、窒素精留塔１８の棚段を増
せば、同様に粗アルゴン中の窒素を減らすことが
できる。さらに、上記実施例では複式精留塔を用
いた例を示したが、これに限らず、下部に酸素を
発生する単式精留塔を用いた場合にも適用でき、
粗アルゴン塔４の凝縮器８の冷媒を液体空気でな
く液体窒素を用いてもよい。 The amount of liquid nitrogen introduced into the nitrogen rectification column 18 may be about the same amount as the crude argon obtained, but if this amount is increased, the amount of nitrogen in the crude argon can be reduced. Further, by increasing the number of plates in the nitrogen rectification column 18, nitrogen in the crude argon can be similarly reduced. Furthermore, although the above embodiment shows an example using a double-type rectification column, the application is not limited to this, but can also be applied to a case where a single-type rectification column that generates oxygen at the bottom is used.
Instead of liquid air, liquid nitrogen may be used as the refrigerant in the condenser 8 of the crude argon column 4.
以上説明したように、この発明のアルゴン製造
装置は粗アルゴン塔上部に新しく窒素精留塔を設
け、この窒素精留塔上部に、中圧塔上部から液体
窒素を還流液として直接導入するように構成した
ものであるので、窒素分の多いフイードガスが粗
アルゴン塔に供給されても、粗アルゴン塔を安定
して運転することができるため、低圧塔の中下部
のアルゴン含有量が最大のところよりフイードガ
スを受けることができ、従つてアルゴンの収率を
向上せしめることができる。また、窒素精留塔上
部に導入する液体窒素の量は得られる粗アルゴン
と略等量でよいので低圧塔の精留にほとんど影響
を与えることがなく、主製品の酸素の採取量を減
らすことなくアルゴン収率を向上できる。更に、
フイードガス中の窒素が外乱などにより多くなる
と従来の装置では粗アルゴン塔の凝縮器が働かな
くなり製品酸素の純度を低下させると言う欠点が
あつたが、この発明の装置においてはかかる欠点
がなく、運転上の不安が解消されるなどの利点を
有する。 As explained above, in the argon production apparatus of the present invention, a new nitrogen rectification column is installed in the upper part of the crude argon column, and liquid nitrogen is directly introduced into the upper part of the nitrogen rectification column as a reflux liquid from the upper part of the medium pressure column. This structure allows the crude argon column to operate stably even if feed gas with a high nitrogen content is supplied to the crude argon column. Feed gas can be received and therefore the yield of argon can be improved. In addition, since the amount of liquid nitrogen introduced into the upper part of the nitrogen rectification column is approximately equal to the amount of crude argon obtained, it has almost no effect on the rectification in the low-pressure column, and the amount of oxygen extracted as the main product can be reduced. The argon yield can be improved without any problems. Furthermore,
Conventional equipment had the disadvantage that when nitrogen in the feed gas increased due to disturbance, etc., the condenser in the crude argon column stopped working, reducing the purity of the product oxygen. However, the apparatus of the present invention does not have this drawback, and the operation It has the advantage of eliminating the above concerns.
以下、この発明のアルゴンの製造装置の操業例
について説明する。 Hereinafter, an example of operation of the argon production apparatus of the present invention will be explained.
第２図に示した装置を用いて、以下の操業条件
でアルゴンを製造した。
Argon was produced using the apparatus shown in FIG. 2 under the following operating conditions.
・ 粗アルゴン塔４へのフイードガス量
：15570Nm3／ｈ
・ 上記フイードガスの組成
：アルゴン13.6vol％
窒 素 5300ppm
酸 素 残部
・ 窒素精留塔１８への液体窒素供給量
：500Nm3／ｈ
以上の条件により運転したところ、
・ 粗アルゴン回収量：600Nm3／ｈ
・ 粗アルゴンの組成：アルゴン 95.5vol％
酸 素 2.0vol％
窒 素 2.5vol％
の運転結果を得、中圧塔５、低圧塔２は安定に操
業することができた。従来の装置でフイードガス
中の窒素を4300ppmとし、粗アルゴンを600N
m3／ｈ回収すると粗アルゴン中の窒素が8vol％を
起え、凝縮器８は温度差がとれず運転不能となつ
てしまう。しかるに本発明では窒素5300ppmある
にかかわらず粗アルゴン中の窒素分を2.5％にお
さえることができ、従来通りの運転ができる。ま
た、フイードガスを同じ15570Nm3／ｈに抑えた
場合、従来の装置では粗アルゴンを555Nm3／ｈ
しか採取できず、この発明によつてアルゴン収率
を著るしく向上できる。- Feed gas amount to crude argon column 4: 15570Nm 3 /h - Composition of the above feed gas
: Argon 13.6vol% Nitrogen 5300ppm Oxygen Remaining liquid nitrogen supply amount to nitrogen rectification column 18: 500Nm 3 /h When operated under the above conditions, - Amount of crude argon recovered: 600Nm 3 /h - Crude argon Composition: Argon 95.5vol%, Oxygen 2.0vol%, Nitrogen 2.5vol% were obtained, and medium pressure column 5 and low pressure column 2 were able to operate stably. With conventional equipment, the nitrogen in the feed gas is 4300ppm and the crude argon is 600N.
If m 3 /h is recovered, nitrogen in the crude argon will increase to 8 vol %, and the condenser 8 will not be able to maintain a temperature difference and will be unable to operate. However, in the present invention, the nitrogen content in the crude argon can be kept to 2.5% even though the nitrogen content is 5300 ppm, and the operation can be carried out as before. Furthermore, when the feed gas is kept at the same level of 15,570Nm 3 /h, the conventional equipment reduces the crude argon to 555Nm 3 /h.
This invention can significantly improve the argon yield.
第１図は従来のアルゴンの製造装置の一例を示
す工程図、第２図はこの発明のアルゴンの製造装
置の一例を示す工程図、第３図は窒素精留塔内の
アルゴン―窒素組成とアルゴン固化点と操作温度
の関係を示すグラフである。
１……複式精留塔、４……粗アルゴン塔、１８
……窒素精留塔、１９……管、２０……弁。
Fig. 1 is a process diagram showing an example of a conventional argon production equipment, Fig. 2 is a process diagram showing an example of an argon production equipment of the present invention, and Fig. 3 is a diagram showing the argon-nitrogen composition in the nitrogen rectification column. It is a graph showing the relationship between argon solidification point and operating temperature. 1...Double rectification column, 4...Crude argon column, 18
...Nitrogen rectification column, 19...pipe, 20...valve.
Claims (1)
装置において、粗アルゴン塔上部に窒素精留塔を
設けると共に該窒素精留塔頂部へ液化窒素を還流
液として導入するように構成したことを特徴とす
るアルゴンの製造装置。1. An apparatus for producing argon by an air liquefaction rectification method, characterized in that a nitrogen rectification column is provided at the top of the crude argon column, and liquefied nitrogen is introduced into the top of the nitrogen rectification column as a reflux liquid. Argon manufacturing equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP55136111A JPS5760166A (en) | 1980-09-30 | 1980-09-30 | Argon producing apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP55136111A JPS5760166A (en) | 1980-09-30 | 1980-09-30 | Argon producing apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5760166A JPS5760166A (en) | 1982-04-10 |
| JPS6333066B2 true JPS6333066B2 (en) | 1988-07-04 |
Family
ID=15167543
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP55136111A Granted JPS5760166A (en) | 1980-09-30 | 1980-09-30 | Argon producing apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5760166A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103267403A (en) * | 2013-05-15 | 2013-08-28 | 兖矿集团有限公司 | Method and system for increasing yield of liquid argon |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58190680A (en) * | 1982-04-30 | 1983-11-07 | 日本酸素株式会社 | Method of liquefying and separating air |
| JPH0534285Y2 (en) * | 1987-02-05 | 1993-08-31 | ||
| CA1293275C (en) * | 1988-01-19 | 1991-12-17 | Ronald Zander | Deflector ring for use with inflators for passive restraint devices |
| JPH0650267Y2 (en) * | 1989-01-18 | 1994-12-21 | 芦森工業株式会社 | Structure of the attachment part of the bag in the airbag device |
| JP2526139B2 (en) * | 1989-11-02 | 1996-08-21 | 池田物産株式会社 | Airbag device |
| CN107580670B (en) * | 2015-03-13 | 2020-02-28 | 林德股份公司 | Apparatus for producing oxygen by cryogenic air separation |
-
1980
- 1980-09-30 JP JP55136111A patent/JPS5760166A/en active Granted
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103267403A (en) * | 2013-05-15 | 2013-08-28 | 兖矿集团有限公司 | Method and system for increasing yield of liquid argon |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5760166A (en) | 1982-04-10 |
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