JPS648271B2 - - Google Patents
Info
- Publication number
- JPS648271B2 JPS648271B2 JP17142979A JP17142979A JPS648271B2 JP S648271 B2 JPS648271 B2 JP S648271B2 JP 17142979 A JP17142979 A JP 17142979A JP 17142979 A JP17142979 A JP 17142979A JP S648271 B2 JPS648271 B2 JP S648271B2
- Authority
- JP
- Japan
- Prior art keywords
- crude argon
- gas
- heat exchanger
- argon
- liquid
- 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 198
- 229910052786 argon Inorganic materials 0.000 claims description 99
- 239000007788 liquid Substances 0.000 claims description 40
- 230000002441 reversible effect Effects 0.000 claims description 35
- 239000007789 gas Substances 0.000 claims description 31
- 238000000926 separation method Methods 0.000 claims description 15
- 238000000034 method Methods 0.000 claims description 14
- 239000012530 fluid Substances 0.000 claims description 13
- 238000010438 heat treatment Methods 0.000 claims description 10
- 238000000605 extraction Methods 0.000 claims 1
- 238000005070 sampling Methods 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 18
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 9
- 239000001301 oxygen Substances 0.000 description 9
- 229910052760 oxygen Inorganic materials 0.000 description 9
- 229910052757 nitrogen Inorganic materials 0.000 description 8
- 238000003303 reheating Methods 0.000 description 4
- 230000007423 decrease Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 229910001882 dioxygen Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000010349 pulsation Effects 0.000 description 1
- 238000000746 purification 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
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
-
- 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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/04096—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of argon or argon enriched stream
-
- 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
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
-
- 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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
- F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
-
- 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
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low 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
- F25J3/04406—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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
-
- 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
- F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
-
- 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
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/40—One fluid being air
-
- 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
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude oxygen"
-
- 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
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/58—One fluid being argon or crude argon
-
- 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
- F25J2290/62—Details of storing a fluid in a tank
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
【発明の詳細な説明】
本発明は空気分離装置におけるアルゴンの採取
方法に係り、液状の粗アルゴンを必要な圧力に高
めた後、安定した状態で気化し、次いで有利に常
温まで加熱する方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for extracting argon in an air separation device, and relates to a method for raising liquid crude argon to the required pressure, vaporizing it in a stable state, and then heating it advantageously to room temperature. .
空気分離装置よりアルゴンを採取するには、空
気を液化精溜して酸素と窒素に分離し、アルゴン
濃度の高い酸素を精溜して粗アルゴンを得、この
粗アルゴンを液状又はガス状で加圧した後、常温
まで加温して酸素除去を行う。次いでこれを精溜
して窒素等と分離し高純アルゴンを得るのが普通
であるが、このうち粗アルゴンを加圧し、かつ加
温するまでの工程を第１図を参照して説明する
と、原料空気は、管１より切換弁２のうちの２ｂ
を介して可逆式熱交換器３の通路３Ａを通り分離
低温ガス等との熱交換により冷却精製された後、
管４、切換弁５、管７を介して複式精溜塔８の下
部塔９の下部に導入されて下部塔９及び上部塔１
０において酸素と窒素に精溜分離される。上部塔
１０の中段にはアルゴン濃度約10％、酸素約90
％、窒素微量のアルゴン・酸素混合ガスがたま
り、これは管１１より粗アルゴン塔１２に吸引さ
れ、下部塔９より管１３、弁１４、加圧器１５、
管１６を経て凝縮器１７に供給される液体空気に
よつて粗アルゴン塔１２内で精溜され、また、凝
縮器１７に供給されかつ気化した空気は管１８よ
り上部塔１０に返送される。精溜により得られた
アルゴン濃度約97％の液体粗アルゴンは粗アルゴ
ン塔１２上部より管１９により導出されて加圧器
１５に導入され該加圧器１５内の液粗アルゴンの
自重による圧力を利用して１〜２Kg／cm2Ｇに加圧
される。加圧された粗アルゴンは、管２０より蒸
発器２１を通り前記可逆式熱交換器３の再熱用通
路３Ｄの中間部より管２２を介して抽出された約
−98℃の中圧空気との熱交換により気化され、次
いで管２３より粗アルゴン熱交換器２４に導入さ
れ、前記可逆式熱交換器３の再熱用通路３Ｄの温
端部から管２５を介して導出された中圧空気との
熱交換により常温まで加熱された後、管２６より
図示しない脱酸器に導入されて粗アルゴンガス中
の酸素が除去される。また、蒸発器２１で粗アル
ゴンと熱交換した後管２７より導出された中圧空
気と、粗アルゴン熱交換器２４で粗アルゴンガス
と熱交換した後管２８より導出された中圧空気
は、合流して管２９より膨張タービン３０に導入
され断熱膨張した後、管３１より寒冷を与えるた
めに前記複式精溜塔８の上部塔１０に導入され
る。 To collect argon from an air separation device, air is liquefied and rectified to separate it into oxygen and nitrogen, oxygen with a high argon concentration is rectified to obtain crude argon, and this crude argon is processed in liquid or gaseous form. After pressurizing, oxygen is removed by heating to room temperature. This is then usually rectified and separated from nitrogen, etc. to obtain highly pure argon, but the process of pressurizing and heating the crude argon will be explained with reference to Figure 1. Raw air is supplied from pipe 1 to 2b of switching valve 2.
After passing through the passage 3A of the reversible heat exchanger 3 and being cooled and purified by heat exchange with separated low-temperature gas, etc.,
It is introduced into the lower part of the lower column 9 of the double rectification column 8 through the pipe 4, the switching valve 5, and the pipe 7, and the lower column 9 and the upper column 1 are
At 0, it is rectified and separated into oxygen and nitrogen. In the middle stage of the upper column 10, the argon concentration is approximately 10%, and the oxygen concentration is approximately 90%.
%, nitrogen, a trace amount of argon/oxygen mixed gas accumulates, which is sucked into the crude argon column 12 through a pipe 11, and then from the lower column 9 through a pipe 13, a valve 14, a pressurizer 15,
The liquid air supplied to the condenser 17 via the pipe 16 is rectified in the crude argon column 12, and the vaporized air supplied to the condenser 17 is returned to the upper column 10 via the pipe 18. Liquid crude argon with an argon concentration of about 97% obtained by rectification is led out from the upper part of the crude argon column 12 through a pipe 19 and introduced into a pressurizer 15, where the pressure due to the dead weight of the liquid crude argon in the pressurizer 15 is utilized. It is pressurized to 1 to 2 kg/cm 2 G. The pressurized crude argon passes through the evaporator 21 from the pipe 20 and is extracted from the intermediate part of the reheating passage 3D of the reversible heat exchanger 3 via the pipe 22 with medium pressure air of about -98°C. Medium-pressure air is vaporized by heat exchange, then introduced into the crude argon heat exchanger 24 through the pipe 23, and led out through the pipe 25 from the warm end of the reheat passage 3D of the reversible heat exchanger 3. After being heated to room temperature by heat exchange with the crude argon gas, the crude argon gas is introduced into a deoxidizer (not shown) through a pipe 26 to remove oxygen from the crude argon gas. In addition, the medium pressure air led out from the tube 27 after heat exchanged with crude argon in the evaporator 21, and the medium pressure air led out from the tube 28 after heat exchanged with crude argon gas in the crude argon heat exchanger 24, After converging, they are introduced into an expansion turbine 30 through a pipe 29, where they are adiabatically expanded, and then introduced through a pipe 31 into the upper column 10 of the double rectification column 8 in order to provide cooling.
なお、図中３３は前記管７より分岐した管で、
この管３３より冷却精製後の原料空気の一部が前
記可逆式熱交換器３の再熱用通路３Ｄに返送され
る。また、３４は前記上部塔１０の下部より製品
酸素ガスを導出する管で、導出された製品酸素ガ
スはこの管３４を通つて前記可逆式熱交換器３の
通路３Ｂに導入されて常温まで加熱された後管３
５より製品として採取される。また、３６は前記
上部塔１０の頂部より不純窒素ガスを導出する管
で、導出された不純窒素ガスはこの管３６を通り
切換弁３７を経て前記可逆式熱交換器３の通路３
Ｃに導入され該通路３Ｃ内に析出した水分、炭酸
ガスを同伴して管３８より外部に排出される。ま
た、３９は前記下部塔９の底部に溜つた液体空気
を前記上部塔１０に供給するための管であり、ま
た４０は前記下部塔９の上部から液体窒素を導出
してこれを前記上部塔１０に供給する管である。 In addition, 33 in the figure is a pipe branched from the pipe 7,
A part of the raw material air after cooling and purification is returned from this pipe 33 to the reheating passage 3D of the reversible heat exchanger 3. Further, 34 is a pipe for leading out the product oxygen gas from the lower part of the upper column 10, and the led out product oxygen gas is introduced into the passage 3B of the reversible heat exchanger 3 through this pipe 34 and heated to room temperature. After the tube 3
It is collected as a product from 5. Further, 36 is a pipe for leading out impure nitrogen gas from the top of the upper column 10, and the led out impure nitrogen gas passes through this pipe 36, passes through a switching valve 37, and then passes through the passage 3 of the reversible heat exchanger 3.
C, and is discharged to the outside from the pipe 38 along with moisture and carbon dioxide that have precipitated in the passage 3C. Further, 39 is a pipe for supplying the liquid air accumulated at the bottom of the lower column 9 to the upper column 10, and 40 is a pipe for drawing out liquid nitrogen from the upper part of the lower column 9 and transferring it to the upper column. 10.
上記のように粗アルゴン塔１２より粗アルゴン
を液状で抜き出し、これを蒸発気化せしめる方式
を採用した場合、加圧器１５で加圧された液状の
粗アルゴンを蒸発器２１で全量気化してガス状で
抜き出そうとすると、粗アルゴンの圧力の脈動及
び出口温度の変動が生じて安定した運転ができな
いという問題がある。 When a method is adopted in which crude argon is extracted in liquid form from the crude argon column 12 and evaporated as described above, the liquid crude argon pressurized in the pressurizer 15 is completely vaporized in the evaporator 21 and converted into gas. If an attempt is made to extract the crude argon, there is a problem that pulsations in the pressure of the crude argon and fluctuations in the outlet temperature occur, making stable operation impossible.
また、可逆式熱交換器３の再熱用通路３Ｄの中
間部より管２２を介して抽出される中圧空気の温
度は可逆式熱交換器３の運転上簡単に変更でき
ず、このため、空気分離装置の減量運転にともな
つて前記中圧空気量が減少した場合には、蒸発器
２１から出る粗アルゴンの出口温度かあるいは中
圧空気の出口温度を大巾に変える必要がある。し
かし、このようにすることは空気分離装置を安定
した状態で運転する際の障害となるが、従来は中
圧空気の出口温度を変えて粗アルゴンを気液混合
状態で蒸発器２１から抜き出し、これをそのまま
粗アルゴン熱交換器２４に導入し気化されないで
残つた液状の粗アルゴンを気化していた。このた
め、粗アルゴン熱交換器２４から出る粗アルゴン
ガスの出口温度が低い不都合が生ずる。 Further, the temperature of the medium pressure air extracted from the middle part of the reheating passage 3D of the reversible heat exchanger 3 via the pipe 22 cannot be easily changed due to the operation of the reversible heat exchanger 3. When the amount of medium pressure air decreases due to the reduced operation of the air separation device, it is necessary to drastically change the outlet temperature of the crude argon or the medium pressure air exiting from the evaporator 21. However, doing this poses an obstacle when operating the air separation device in a stable state. Conventionally, crude argon is extracted from the evaporator 21 in a gas-liquid mixed state by changing the outlet temperature of the medium-pressure air. This was directly introduced into the crude argon heat exchanger 24, and the liquid crude argon that remained without being vaporized was vaporized. For this reason, a disadvantage arises in that the outlet temperature of the crude argon gas coming out of the crude argon heat exchanger 24 is low.
また、粗アルゴン熱交換器２４における加熱流
体である中圧空気は可逆式熱交換器１１及び粗ア
ルゴン熱交換器２４を通ることにより圧力損失が
大きく、このため、一般に該中圧空気の下流に設
けられる膨張タービン３０の入口圧力を低下させ
る問題がある。 In addition, the medium pressure air that is the heating fluid in the crude argon heat exchanger 24 has a large pressure loss as it passes through the reversible heat exchanger 11 and the crude argon heat exchanger 24, and therefore, generally, the pressure loss is large in the downstream of the medium pressure air. There is a problem of reducing the inlet pressure of the expansion turbine 30 provided.
本発明は上記事情に鑑みてなされたもので、そ
の目的とするところは、蒸発器を安定した状態で
運転させることができる上に、空気分離装置の減
量運転時において支障が生じるようなことがな
く、また膨張タービンの入口圧力が低下するよう
なことのない空気分離装置におけるアルゴンの採
取方法を提供することである。 The present invention has been made in view of the above-mentioned circumstances, and its purpose is to enable the evaporator to operate in a stable state and to prevent problems from occurring during the reduction operation of the air separation device. It is an object of the present invention to provide a method for extracting argon in an air separation device that does not cause the inlet pressure of an expansion turbine to decrease.
以下、本発明の実施例を説明する。 Examples of the present invention will be described below.
まず、第２図を参照して本発明の第一実施例を
説明する。なお、第２図中第１図に示す部分と同
一部分には同一符号を付してその説明を省略す
る。可逆式熱交換器３の冷端部から中間部まで延
びる再熱用通路３D1より管４５を介して導出さ
れた約−98℃の中圧空気は、該通路３D1に導入
される前に管３３から分岐した管４６、弁４７を
介して導出された約−173℃の中圧空気が混合さ
れて温度が調整された後、管４８より蒸発器２１
に導入されて粗アルゴンと熱交換される。この中
圧空気の温度は、蒸発器２１の出口において粗ア
ルゴンを気液混合状態に安定させる温度に調整さ
れている。また、空気分離装置の減量運転時には
弁４７を操作して可逆式熱交換器３の通路３D1
に導入される前の約−173℃の中圧空気の混合量
を調整して蒸発器２１の出口にいて粗アルゴンを
気液混合状態に安定させると共に、中圧空気の蒸
発器出口温度を原料空気の増減量にかかわらず安
定させる。粗アルゴンは、これにより一部気化し
て気液混合状態に安定し、蒸発器２１より管４９
を介し気液分離器５０に導入されて粗アルゴンガ
スと液粗アルゴンに分離される。分離された粗ア
ルゴンガスは、約−174℃の状態で気液分離器５
０より管５１を介して導出されて可逆式熱交換器
３の冷端部か温端部まで延びる通路３Ｅを通つて
原料空気との熱交換により常温まで加熱された
後、管５２より図示しない脱酸器に導入されて従
来と同様に酸素分が除去される。また、気液分離
器５０で分離された液粗アルゴンは、管５３を介
して導出され管２０を流れる加圧後の粗アルゴン
に合流して再び蒸発器２１に返送される。 First, a first embodiment of the present invention will be described with reference to FIG. Note that the same parts in FIG. 2 as those shown in FIG. Medium-pressure air at about -98°C is led out from the reheating passage 3D 1 extending from the cold end to the middle part of the reversible heat exchanger 3 via the pipe 45 before being introduced into the passage 3D 1 . Medium-pressure air of approximately -173°C led out through a pipe 46 branched from the pipe 33 and a valve 47 is mixed and the temperature is adjusted, and then the air is sent to the evaporator 21 through a pipe 48.
and heat exchanged with crude argon. The temperature of this medium pressure air is adjusted to a temperature that stabilizes the crude argon in a gas-liquid mixed state at the outlet of the evaporator 21. In addition, during the reduction operation of the air separation device, the passage 3D 1 of the reversible heat exchanger 3 is operated by operating the valve 47.
By adjusting the mixed amount of medium-pressure air of approximately -173°C before being introduced into the evaporator 21, the crude argon is stabilized in a gas-liquid mixed state at the outlet of the evaporator 21, and the temperature of the medium-pressure air at the evaporator outlet is adjusted to match that of the raw material. Stable regardless of increase or decrease of air. As a result, the crude argon is partially vaporized and stabilized in a gas-liquid mixed state.
The gas is introduced into a gas-liquid separator 50 through which it is separated into crude argon gas and liquid crude argon. The separated crude argon gas is passed through the gas-liquid separator 5 at a temperature of approximately -174°C.
After being heated to room temperature by heat exchange with raw air through a passage 3E extending to either the cold end or the hot end of the reversible heat exchanger 3, the air is led out from the pipe 51 through the pipe 52, not shown. It is introduced into a deoxidizer and the oxygen content is removed in the same manner as before. Further, the liquid crude argon separated by the gas-liquid separator 50 is led out through the pipe 53, joins the pressurized crude argon flowing through the pipe 20, and is returned to the evaporator 21 again.
一方、蒸発器２１で熱交換した中圧空気は、蒸
発器２１での出口温度が一定となつた状態で管２
７、管２９より膨張タービン３０に導入される
が、膨張タービン３０での入口温度が低くすぎる
ような場合にはその前に管４５から分岐した管５
４、弁５５を経て可逆式熱交換器３で加熱された
中圧空気が混合される。 On the other hand, the intermediate pressure air that has undergone heat exchange in the evaporator 21 is transferred to the pipe 2 with the outlet temperature of the evaporator 21 being constant.
7. It is introduced into the expansion turbine 30 through the pipe 29, but if the inlet temperature at the expansion turbine 30 is too low, the pipe 5 branched from the pipe 45 is introduced beforehand.
4. Medium pressure air heated by the reversible heat exchanger 3 is mixed through the valve 55.
なお、上記中圧空気は、可逆式熱交換器３の温
度制御を受けもつものであり、同様な働きは中圧
低純窒素や中圧窒素もするので、中圧空気に代え
てこれら中圧低純窒素等を使用しても同じ効果が
得られる。 Note that the medium pressure air mentioned above is responsible for temperature control of the reversible heat exchanger 3, and medium pressure low purity nitrogen and medium pressure nitrogen also have a similar function, so these medium pressure air can be used instead of medium pressure air. The same effect can be obtained even if low purity nitrogen or the like is used.
次に第３図を参照して本発明の第二の実施例を
説明する。なお、第３図中第１図及び第２図に示
す部分と同一部分には同一符号を付してその説明
を省略する。この第二実施例にあつては、気液分
離器５０で分離された粗アルゴンガスの加熱方法
が前述の第一実施例の場合と異なつている。すな
わち、気液分離器５０で分離された粗アルゴンガ
スは、管５６を介して導出されて粗アルゴン熱交
換器５７に導入されて管４５から分岐した管５
８、弁５９を介して導出された中圧空気との熱交
換により−100℃〜−120℃まで加熱された後、管
６０より可逆式熱交換器３の中間部から温端部ま
で延びる通路３D2に導入されて原料空気との熱
交換により常温まで加熱されて管６１より図示し
ない脱酸器に送られ、従来と同様に酸素分が除去
される。 Next, a second embodiment of the present invention will be described with reference to FIG. Note that the same parts in FIG. 3 as those shown in FIGS. 1 and 2 are designated by the same reference numerals, and their explanations will be omitted. In this second embodiment, the method of heating the crude argon gas separated by the gas-liquid separator 50 is different from that in the first embodiment. That is, the crude argon gas separated by the gas-liquid separator 50 is led out through a pipe 56 and introduced into a crude argon heat exchanger 57, and then transferred to a pipe 5 branched from the pipe 45.
8. A passage extending from the middle part of the reversible heat exchanger 3 to the hot end from the pipe 60 after being heated to -100°C to -120°C by heat exchange with medium pressure air led out through the valve 59. The air is introduced into 3D 2 and heated to room temperature through heat exchange with raw air, and then sent through a pipe 61 to a deoxidizer (not shown), where oxygen is removed in the same manner as in the conventional case.
一方、粗アルゴン熱交換器５７で粗アルゴンガ
スと熱交換した中圧空気は、管６２を通つて管２
７に流れる中圧空気と合流して管２９より膨張タ
ービン３０に導入される。 On the other hand, the intermediate pressure air that has undergone heat exchange with the crude argon gas in the crude argon heat exchanger 57 passes through the pipe 62 and passes through the pipe 2.
It joins with the intermediate pressure air flowing through the pipe 7 and is introduced into the expansion turbine 30 through the pipe 29.
なお、以上の実施例においては、液状の粗アル
ゴンを加圧する手段として加圧塔を用いている
が、これは液ポンプ等機械的手段による場合にも
適用できる。 In the above embodiments, a pressurizing tower is used as a means for pressurizing liquid crude argon, but this can also be applied to mechanical means such as a liquid pump.
以上説明したように本発明によれば、蒸発器に
おいて温度調整された中圧流体との熱交換により
粗アルゴンを気液混合状態に安定させ、この粗ア
ルゴンを気液分離器に導入して粗アルゴンガスと
液粗アルゴンとに分離し、粗アルゴンガスを常温
まで加熱している。したがつて、蒸発器に起因す
る粗アルゴンの圧力及び温度の変動を防止し得、
蒸発器を安定した状態で運転できる。また、空気
分離装置の減量運転時や増量運転時においても、
蒸発器において加熱流体となる中圧流体の温度を
調整することにより、蒸発器から出る粗アルゴン
の出口温度及び中圧空気の出口温度を安定させる
ことができる。また、粗アルゴンを充分加温した
状態で得られ、従来のように温度が低下した粗ア
ルゴンガスを次工程へ供給することの不都合を解
消できる。 As explained above, according to the present invention, crude argon is stabilized in a gas-liquid mixed state by heat exchange with a medium-pressure fluid whose temperature has been adjusted in an evaporator, and this crude argon is introduced into a gas-liquid separator to produce crude argon. Argon gas and liquid crude argon are separated, and the crude argon gas is heated to room temperature. Therefore, fluctuations in the pressure and temperature of crude argon due to the evaporator can be prevented;
The evaporator can be operated in stable conditions. In addition, even when the air separation equipment is operating at reduced capacity or increased capacity,
By adjusting the temperature of the medium-pressure fluid serving as the heating fluid in the evaporator, the outlet temperature of crude argon and the medium-pressure air exiting from the evaporator can be stabilized. Further, the crude argon is obtained in a sufficiently heated state, and the disadvantage of supplying crude argon gas whose temperature has been lowered to the next step as in the conventional method can be eliminated.
また、本発明によれば、粗アルゴンガスを加熱
するのに、可逆式熱交換器の冷端部から温端部ま
で流して加熱するか、または可逆式熱交換器の中
間部から導出した中圧流体の一部を利用して粗ア
ルゴン熱交換器でいつたん予備加熱した後、可逆
式熱交換器の中間部から温端部まで流して加熱し
ている。したがつて、従来の如く、可逆式熱交換
器の温端部より導出した中圧流体を利用する場合
の如く、膨張タービンの入口圧力を必要以上に低
下させるおそれがない。また、粗アルゴンガスを
加熱するのに、粗アルゴンガスを可逆式熱交換器
の冷端部から温端部まで流して加熱する場合に
は、熱交換器を１個省略することができ、また可
逆式熱交換器に流す粗アルゴンガス量は原料空気
量に比して非常に少なく粗アルゴンガスを流すた
めにあえて可逆式熱交換器を大きくする必要がな
く、このため、設備費を安価におさえることがで
きる。 Further, according to the present invention, crude argon gas can be heated by flowing it from the cold end to the warm end of the reversible heat exchanger, or by heating the crude argon gas by flowing it from the middle part of the reversible heat exchanger. A portion of the pressurized fluid is temporarily preheated in a crude argon heat exchanger, and then heated by flowing from the middle to the hot end of the reversible heat exchanger. Therefore, there is no risk of lowering the inlet pressure of the expansion turbine more than necessary, unlike in the conventional case where intermediate pressure fluid led out from the hot end of the reversible heat exchanger is used. In addition, when crude argon gas is heated by flowing it from the cold end to the warm end of a reversible heat exchanger, one heat exchanger can be omitted, and The amount of crude argon gas flowing through the reversible heat exchanger is very small compared to the amount of raw air, so there is no need to make the reversible heat exchanger larger in order to flow the crude argon gas, which reduces equipment costs. It can be suppressed.
第１図は従来法の工程図、第２図は本発明の第
一実施例を示す工程図、第３図は本発明の第二実
施例を示す工程図である。
３……可逆式熱交換器、１５……加圧器、２１
……蒸発器、５０……気液分離器、５７……粗ア
ルゴン熱交換器、３D1，３D2，３Ｅ……通路。
FIG. 1 is a process diagram of a conventional method, FIG. 2 is a process diagram of a first embodiment of the present invention, and FIG. 3 is a process diagram of a second embodiment of the present invention. 3... Reversible heat exchanger, 15... Pressurizer, 21
... Evaporator, 50 ... Gas-liquid separator, 57 ... Crude argon heat exchanger, 3D 1 , 3D 2 , 3E ... Passage.
Claims (1)
装置を附設してなる空気分離装置の粗アルゴン塔
で得られた液状の粗アルゴンを、必要な圧力に高
めた後、蒸発器において前記可逆式熱交換器の中
間部から導出した該可逆式熱交換器の温度制御用
の中圧流体に該中圧流体の可逆式熱交換器に導入
される前のものを混合して温度を調整した混合中
圧流体との熱交換により一部気化して気液混合状
態にし、この気液混合状態の粗アルゴンを気液分
離器において粗アルゴンガスと液粗アルゴンとに
分離し、該粗アルゴンガスを常温まで加熱するこ
とを特徴とする空気分離装置におけるアルゴンの
採取方法。 ２ 前記気液分離器で分離された液粗アルゴン
を、前記蒸発器に導入する前の液状粗アルゴンに
返送することを特徴とする特許請求の範囲第１項
記載の空気分離装置におけるアルゴンの採取方
法。 ３ 前記粗アルゴンガスの常温までの加熱が、粗
アルゴンガスを前記可逆式熱交換器の冷端部から
温端部まで流して原料空気との熱交換により加熱
することを特徴とする特許請求の範囲第１項記載
の空気分離装置におけるアルゴンの採取方法。 ４ 可逆式熱交換器を採用し、かつアルゴン採取
装置を附設してなる空気分離装置の粗アルゴン塔
で得られた液状粗アルゴンを、必要な圧力に高め
た後、蒸発器において前記可逆式熱交換器の中間
部から導出した該可逆式熱交換器の温度制御用の
中圧流体の一部に該中圧流体の可逆式熱交換器に
導入される前のものを混合して温度を調整した混
合中圧流体との熱交換により一部気化して気液混
合状態にし、この気液混合状態の粗アルゴンを気
液分離器において粗アルゴンガスと液粗アルゴン
とに分離し、該粗アルゴンガスを粗アルゴン熱交
換器において前記可逆式熱交換器の中間部から導
出した中圧流体の残部との熱交換により加熱した
後、前記可逆式熱交換器の中間部から温端部まで
流して原料空気との熱交換により常温まで加熱す
ることを特徴とする空気分離装置におけるアルゴ
ンの採取方法。 ５ 前記粗アルゴンガスを、粗アルゴン熱交換器
において前記可逆式熱交換器の中間部から導出し
た中圧流体との熱交換により−100℃〜−120℃ま
で加熱することを特徴とする特許請求の範囲第４
項記載の空気分離装置におけるアルゴンの採取方
法。[Claims] 1. After raising the liquid crude argon obtained in the crude argon column of the air separation device which employs a reversible heat exchanger and is equipped with an argon sampling device to the required pressure, In the evaporator, the intermediate pressure fluid for temperature control of the reversible heat exchanger drawn out from the intermediate part of the reversible heat exchanger is mixed with the intermediate pressure fluid before being introduced into the reversible heat exchanger. The crude argon is partially vaporized by heat exchange with a mixed intermediate pressure fluid whose temperature has been adjusted to form a gas-liquid mixed state, and the crude argon in the gas-liquid mixed state is separated into crude argon gas and liquid crude argon in a gas-liquid separator. A method for collecting argon in an air separation device, which comprises heating the crude argon gas to room temperature. 2. Collection of argon in the air separation apparatus according to claim 1, characterized in that the liquid crude argon separated by the gas-liquid separator is returned to the liquid crude argon before being introduced into the evaporator. Method. 3. The crude argon gas is heated to room temperature by flowing the crude argon gas from the cold end to the hot end of the reversible heat exchanger and heating it by heat exchange with raw air. A method for collecting argon in the air separation device according to scope 1. 4. After increasing the liquid crude argon obtained in the crude argon column of the air separation device which employs a reversible heat exchanger and is equipped with an argon extraction device to the required pressure, the reversible heat is transferred to the evaporator. Temperature is adjusted by mixing a portion of the intermediate pressure fluid for temperature control of the reversible heat exchanger derived from the middle part of the exchanger with the intermediate pressure fluid before being introduced into the reversible heat exchanger. The crude argon in the gas-liquid mixed state is separated into crude argon gas and liquid crude argon in a gas-liquid separator, and the crude argon is separated into crude argon gas and liquid crude argon. After the gas is heated in a crude argon heat exchanger by heat exchange with the remainder of the medium pressure fluid drawn out from the middle part of the reversible heat exchanger, the gas is passed from the middle part to the hot end of the reversible heat exchanger. A method for collecting argon in an air separation device, which is characterized by heating to room temperature by heat exchange with raw air. 5. A patent claim characterized in that the crude argon gas is heated to −100° C. to −120° C. in a crude argon heat exchanger by heat exchange with medium-pressure fluid derived from an intermediate portion of the reversible heat exchanger. range 4th
Method for collecting argon in the air separation device described in Section 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP17142979A JPS5697774A (en) | 1979-12-29 | 1979-12-29 | Method of sampling argon in air separator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP17142979A JPS5697774A (en) | 1979-12-29 | 1979-12-29 | Method of sampling argon in air separator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5697774A JPS5697774A (en) | 1981-08-06 |
| JPS648271B2 true JPS648271B2 (en) | 1989-02-13 |
Family
ID=15922960
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP17142979A Granted JPS5697774A (en) | 1979-12-29 | 1979-12-29 | Method of sampling argon in air separator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5697774A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58155593U (en) * | 1982-04-13 | 1983-10-18 | 日本酸素株式会社 | Air liquefaction separation equipment |
| DE3428968A1 (en) * | 1984-08-06 | 1986-02-13 | Linde Ag, 6200 Wiesbaden | METHOD AND DEVICE FOR DISASSEMBLING ROHARGON |
-
1979
- 1979-12-29 JP JP17142979A patent/JPS5697774A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5697774A (en) | 1981-08-06 |
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