JPS6142072Y2 - - Google Patents
Info
- Publication number
- JPS6142072Y2 JPS6142072Y2 JP1981021056U JP2105681U JPS6142072Y2 JP S6142072 Y2 JPS6142072 Y2 JP S6142072Y2 JP 1981021056 U JP1981021056 U JP 1981021056U JP 2105681 U JP2105681 U JP 2105681U JP S6142072 Y2 JPS6142072 Y2 JP S6142072Y2
- Authority
- JP
- Japan
- Prior art keywords
- argon
- flow path
- condenser
- crude argon
- refrigerant
- 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 104
- 229910052786 argon Inorganic materials 0.000 claims description 52
- 239000003507 refrigerant Substances 0.000 claims description 24
- 239000007789 gas Substances 0.000 claims description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 18
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- 239000007788 liquid Substances 0.000 description 8
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 4
- 238000010926 purge Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 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
- F25J3/044—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 single pressure main column system only
-
- 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
- F25J3/04624—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 integrated mass and heat exchange, so-called non-adiabatic rectification, e.g. dephlegmator, reflux exchanger
-
- 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
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
- F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
- F25J5/005—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger in a reboiler-condenser, e.g. within a 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
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
- F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
- F25J5/007—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger combined with mass exchange, i.e. in a so-called dephlegmator
-
- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
-
- 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
-
- 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/04—Down-flowing type boiler-condenser, i.e. with evaporation of a falling liquid film
-
- 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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
【考案の詳細な説明】
この考案は空気液化分離装置の粗アルゴン塔用
凝縮器に関するものである。[Detailed Description of the Invention] This invention relates to a condenser for a crude argon column in an air liquefaction separation device.
従来の粗アルゴン塔用凝縮器は、第１図に示し
た直管式の熱交換部１や第２図に示したプレート
フイン式の熱交換部２を粗アルゴン塔３の上部に
設けられた液化空気溜４中に浸漬し、前記熱交換
部１，２のアルゴン流部５に粗アルゴン塔３の下
部より上昇してくるアルゴン含有ガスを導入し、
該流路５で凝縮させる構造のものが普通である。
このような構造のものにあつては凝縮器で液化空
気を連続して蒸発させているため、液化空気中に
極く微量含有されているアセチレンが液化空気溜
４の液化空気中に徐々に濃縮し、保安上好ましく
ない。このため、アセチレン濃縮防止と溜る液組
成の調節による凝縮器の温度制御のため液化空気
溜４の底部に設けられた液化空気抜液管６より少
量の液化空気を常時抜き出していた。このため余
分な液化空気を凝縮器に供給していることにな
る。また、第２図のプレートフイン式の熱交換部
２や第３図に示したハンプソン式の熱交換部７を
もつた凝縮器では、その構造上粗アルゴン塔３塔
頂に溜る窒素分を充分にパージすることができな
く、前記熱交換部２，７において必要な温度差を
取りにくくなるため、この窒素分とともに相当量
のアルゴンをパージする必要が生じ貴重なアルゴ
ンを無駄にしていた。窒素分のパージの点からす
ると、第１図に示した直管式の熱交換部１を用い
るものは有利となるが、直管式の熱交換部１はプ
レートフイン式熱交換部２やハンプソン式熱交換
部３に比べて形状が大型となり製作工数も多く、
従つて高価になるという欠点を有していた。 A conventional condenser for a crude argon column has a straight tube type heat exchange section 1 shown in FIG. 1 or a plate fin type heat exchange section 2 shown in FIG. 2 installed at the top of a crude argon column 3. It is immersed in the liquefied air reservoir 4, and the argon-containing gas rising from the lower part of the crude argon column 3 is introduced into the argon flow section 5 of the heat exchange sections 1 and 2,
A structure in which condensation occurs in the flow path 5 is common.
With this type of structure, the liquefied air is continuously evaporated in the condenser, so the acetylene contained in the liquefied air in extremely small amounts is gradually concentrated in the liquefied air in the liquefied air reservoir 4. However, this is not desirable from a security standpoint. For this reason, a small amount of liquefied air is constantly drawn out from the liquefied air drain pipe 6 provided at the bottom of the liquefied air reservoir 4 in order to prevent acetylene concentration and to control the temperature of the condenser by adjusting the composition of the collected liquid. This means that excess liquefied air is being supplied to the condenser. In addition, in the condenser having the plate fin type heat exchange section 2 shown in Fig. 2 or the Hampson type heat exchange section 7 shown in Fig. 3, due to its structure, the nitrogen content accumulated at the top of the crude argon column 3 is sufficiently removed. This makes it difficult to obtain the necessary temperature difference between the heat exchange sections 2 and 7, which necessitates purging a considerable amount of argon along with the nitrogen content, wasting valuable argon. From the point of view of purging nitrogen content, it is advantageous to use the straight tube type heat exchange section 1 shown in Fig. Compared to the type heat exchanger 3, the shape is larger and requires more man-hours to manufacture.
Therefore, it has the disadvantage of being expensive.
この考案は上記事情に鑑みてなされたもので、
粗アルゴン塔凝縮器に供給する液化空気量を減少
でき、粗アルゴン塔塔頂に溜まる窒素分を効果的
にパージでき、かつ熱交換温度差を大きくするこ
とができ、よつて小型で安価な粗アルゴン塔用凝
縮器を提供することを目的とし、粗アルゴン塔上
部に液溜を有しないプレートフイン型熱交換部を
設け、この熱交換部の冷媒流路に冷媒を流して該
流路内で気化状態で導出し、アルゴン流路でアル
ゴン含有ガスを凝縮させて粗アルゴン塔上部に返
戻すると共に該流路温端部より窒素濃度の高いガ
スを導出することを特徴とするものである。 This idea was made in view of the above circumstances,
The amount of liquefied air supplied to the crude argon column condenser can be reduced, the nitrogen content accumulated at the top of the crude argon column can be effectively purged, and the heat exchange temperature difference can be increased. The purpose is to provide a condenser for an argon column, and a plate-fin type heat exchange section without a liquid reservoir is provided in the upper part of the crude argon column. The argon-containing gas is discharged in a vaporized state, condensed in an argon flow path, and returned to the upper part of the crude argon column, and a gas with a high nitrogen concentration is discharged from the hot end of the flow path.
以下、図面を参照してこの考案を詳しく説明す
る。 This invention will be explained in detail below with reference to the drawings.
第４図はこの考案の粗アルゴン塔用凝縮器の実
施例を示すもので、粗アルゴン塔１０の下部に導
入されたアルゴン含有ガスは精留されつつ該塔１
０内を上昇し、粗アルゴン塔１０の塔頂に設けら
れたプレートフイン型の熱交換部をもつた構造で
なる凝縮器１１のアルゴン流路１２に流入する。
一方、凝縮器１１の冷媒流路１３には冷媒導入管
１４を経て下部精留塔（図示せず）より冷媒とし
て液化空気が供給され、冷媒流路１３を流れなが
ら前記アルゴン流路１２を流れるアルゴン含有ガ
スと熱交換する。この結果流入液化空気は全量が
気化し、頂部に設けられ、冷媒流路１３と連通す
る冷媒導出管１５より導出され、上部精溜塔（図
示せず）に返送される。又、液化空気と熱交換し
たアルゴン含有ガスはアルゴン流路１２で液化
し、該流路１２壁面を流下しながら上昇してくる
アルゴン含有ガスと気液接触した後、粗アルゴン
塔１０へ戻され、還流液として該塔１０内を流下
する。また、アルゴン流路１２の頂部には窒素濃
度の高いガスが留り、該流路１２と連通する窒素
パージ管１６より系外に抜き出される。こうして
粗アルゴン塔１０内で精溜が行なわれ、その結果
管１７よりアルゴン濃度95〜98％の粗アルゴンが
抜き出され、次工程に送られる。 FIG. 4 shows an embodiment of the crude argon column condenser of this invention, in which the argon-containing gas introduced into the lower part of the crude argon column 10 is rectified and
0, and flows into the argon flow path 12 of the condenser 11, which has a structure having a plate-fin type heat exchange section provided at the top of the crude argon column 10.
On the other hand, liquefied air is supplied as a refrigerant to the refrigerant flow path 13 of the condenser 11 from a lower rectification column (not shown) via a refrigerant introduction pipe 14, and flows through the argon flow path 12 while flowing through the refrigerant flow path 13. Heat exchange with argon-containing gas. As a result, the entire amount of the inflowing liquefied air is vaporized, led out from the refrigerant outlet pipe 15 provided at the top and communicating with the refrigerant flow path 13, and returned to the upper rectification column (not shown). Further, the argon-containing gas that has exchanged heat with the liquefied air is liquefied in the argon channel 12, comes into gas-liquid contact with the argon-containing gas rising while flowing down the wall surface of the channel 12, and is then returned to the crude argon column 10. , flows down the column 10 as a reflux liquid. Furthermore, gas with a high nitrogen concentration remains at the top of the argon flow path 12 and is extracted from the system through a nitrogen purge pipe 16 communicating with the flow path 12 . In this way, rectification is performed in the crude argon column 10, and as a result, crude argon with an argon concentration of 95 to 98% is extracted from the tube 17 and sent to the next step.
以上のように構成された凝縮器によつて供給さ
れる冷媒液化空気量を調節し、供給冷媒が冷媒流
路１３上部で全量気化するようにすることにより
液化空気中に含有されるアセチレンも同時に気化
せしめるのでアセチレンの濃縮が起らない。ま
た、凝縮に必要な量の液化空気だけを供給すれば
よいので精溜塔の精溜効率を上げることができ
る。また、アルゴン流路１２内で凝縮した凝縮液
とアルゴン含有ガスとが向流し気液接触するの
で、凝縮器１１の頂部より窒素濃度の高いガスを
排出でき、アルゴンのロスを少なくすることがで
きるとともに、熱交換に必要な温度差が取りやす
くなり、小型化できる。さらに、従来の如く冷媒
液溜を設けていないので、液化空気の液深による
温度差減少分を考慮する等の必要がない。なお、
この考案における熱交換態様は第４図に示した構
造のプレートフイン型に限定されず、第２図に示
したプレートフイン型で、冷媒流路側を液溜とせ
ず冷媒を冷媒流路内で完全に気化させる構造のも
のも使用することができる。 By adjusting the amount of refrigerant liquefied air supplied by the condenser configured as described above so that the supplied refrigerant is completely vaporized at the upper part of the refrigerant flow path 13, acetylene contained in the liquefied air is also simultaneously removed. Since it is vaporized, concentration of acetylene does not occur. Further, since it is necessary to supply only the amount of liquefied air necessary for condensation, the rectification efficiency of the rectification column can be increased. In addition, since the condensed liquid condensed in the argon flow path 12 and the argon-containing gas come into counterflow gas-liquid contact, gas with a high nitrogen concentration can be discharged from the top of the condenser 11, and loss of argon can be reduced. At the same time, it becomes easier to take the temperature difference necessary for heat exchange, and the size can be reduced. Furthermore, since no refrigerant reservoir is provided as in the conventional case, there is no need to consider the reduction in temperature difference due to the depth of liquefied air. In addition,
The heat exchange mode in this invention is not limited to the plate-fin type structure shown in Fig. 4, but the plate-fin type shown in Fig. 2, in which the refrigerant is completely absorbed within the refrigerant flow path without forming a liquid reservoir on the refrigerant flow path side. A structure that allows vaporization to occur can also be used.
以上の説明より明らかなように、この考案の粗
アルゴン塔用凝縮器は、液溜を有しないプレート
フイン型熱交換部によつて冷媒を冷媒流路内で完
全気化させるようにしたのでアセチレンの濃縮が
起こらず、従来の如く保安上の問題点がなくな
る。また、凝縮に必要な最少量の冷媒を供給すれ
ばよいので、冷媒として用いられる液化空気量が
減少し、精溜塔の精溜効率が向上し、コスト的に
有利となる。さらに、アルゴン流路温端部より窒
素濃度の高いガスを排出できるので貴重なアルゴ
ンのロスが少なくなり、小型のプレートフイン型
熱交換部で運転できるようになるので、設備費の
低減が可能となるなどのすぐれた利点を有するも
のである。 As is clear from the above explanation, the crude argon column condenser of this invention completely vaporizes the refrigerant within the refrigerant flow path using a plate-fin type heat exchanger that does not have a liquid reservoir. Condensation does not occur, and there are no safety concerns as in the past. Furthermore, since it is only necessary to supply the minimum amount of refrigerant required for condensation, the amount of liquefied air used as a refrigerant is reduced, the rectification efficiency of the rectification column is improved, and it is advantageous in terms of cost. Furthermore, gas with a high nitrogen concentration can be discharged from the hot end of the argon flow path, reducing the loss of valuable argon, and enabling operation with a small plate-fin type heat exchanger, reducing equipment costs. It has excellent advantages such as:
第１図ないし第３図は従来の粗アルゴン塔用凝
縮器を示す概略構成図で、第１図は直管式熱交換
部を、第２図はプレートフイン式熱交換部を、第
３図はハンプソン式熱交換部を有するものをそれ
ぞれ示す。第４図はこの考案の粗アルゴン塔用凝
縮器の一例を示す概略構成図である。
１０……粗アルゴン塔、１１……プレートフイ
ン型熱交換部、１２……アルゴン流路、１３……
冷媒流路。
Figures 1 to 3 are schematic configuration diagrams showing conventional condensers for crude argon columns. Figure 1 shows a straight pipe heat exchange section, Figure 2 shows a plate fin heat exchange section, and Figure 3 shows a plate fin heat exchange section. 1 and 2 respectively indicate those having a Hampson type heat exchange section. FIG. 4 is a schematic diagram showing an example of the crude argon column condenser of this invention. 10... Crude argon column, 11... Plate fin type heat exchange section, 12... Argon channel, 13...
Refrigerant flow path.
Claims (1)
ン塔用凝縮器において、該凝縮器の熱交換部を
アルゴン流路と、冷媒流路とをそれぞれ有する
プレートフイン型に構成し、かつ前記アルゴン
流路の下部を粗アルゴン塔頂部に、又上部を非
凝縮ガス導出管と連通せしめると共に、冷媒流
路の一方を冷媒供給管と、他方を導出管と連通
せしめ、冷媒供給管を介して供給された冷媒が
冷媒流路内で完全気化し導出管より導出するよ
うにしたことを特徴とする粗アルゴン塔用凝縮
器。 (2) 前記粗アルゴン塔頂部よりアルゴン流路を上
昇したアルゴン含有ガスの凝縮液が該流路を流
下して粗アルゴン塔に返戻することを特徴とす
る実用新案登録請求の範囲第１項記載の粗アル
ゴン塔用凝縮器。[Claims for Utility Model Registration] (1) In a crude argon column condenser provided at the top of the crude argon column, the heat exchange section of the condenser is formed by a plate fin having an argon flow path and a refrigerant flow path. The lower part of the argon flow path is connected to the top of the crude argon column, the upper part is connected to the non-condensed gas outlet pipe, and one of the refrigerant flow paths is connected to the refrigerant supply pipe and the other to the outlet pipe. A condenser for a crude argon column, characterized in that a refrigerant supplied through a refrigerant supply pipe is completely vaporized within a refrigerant flow path and is led out from a discharge pipe. (2) Utility model registration claim 1, characterized in that the condensate of the argon-containing gas that has risen through the argon channel from the top of the crude argon column flows down the channel and is returned to the crude argon column. Condenser for crude argon column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1981021056U JPS6142072Y2 (en) | 1981-02-17 | 1981-02-17 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1981021056U JPS6142072Y2 (en) | 1981-02-17 | 1981-02-17 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS57134596U JPS57134596U (en) | 1982-08-21 |
| JPS6142072Y2 true JPS6142072Y2 (en) | 1986-11-29 |
Family
ID=29818944
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1981021056U Expired JPS6142072Y2 (en) | 1981-02-17 | 1981-02-17 |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6142072Y2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1997001068A1 (en) * | 1995-06-20 | 1997-01-09 | Nippon Sanso Corporation | Method and apparatus for separating argon |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4577977B2 (en) * | 2000-11-14 | 2010-11-10 | 大陽日酸株式会社 | Air liquefaction separation method and apparatus |
| JP4520668B2 (en) * | 2001-07-17 | 2010-08-11 | 大陽日酸株式会社 | Air separation method and apparatus |
| EP3133361B1 (en) * | 2015-08-20 | 2018-06-13 | Linde Aktiengesellschaft | Distillation column system and system for the production of oxygen by cryogenic decomposition of air |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5068507A (en) * | 1973-10-23 | 1975-06-07 | ||
| JPS5479007A (en) * | 1977-12-05 | 1979-06-23 | Victor Co Of Japan Ltd | Music selector of tape recorders |
-
1981
- 1981-02-17 JP JP1981021056U patent/JPS6142072Y2/ja not_active Expired
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5068507A (en) * | 1973-10-23 | 1975-06-07 | ||
| JPS5479007A (en) * | 1977-12-05 | 1979-06-23 | Victor Co Of Japan Ltd | Music selector of tape recorders |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1997001068A1 (en) * | 1995-06-20 | 1997-01-09 | Nippon Sanso Corporation | Method and apparatus for separating argon |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS57134596U (en) | 1982-08-21 |
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