JPH0132435B2 - - Google Patents
Info
- Publication number
- JPH0132435B2 JPH0132435B2 JP55079446A JP7944680A JPH0132435B2 JP H0132435 B2 JPH0132435 B2 JP H0132435B2 JP 55079446 A JP55079446 A JP 55079446A JP 7944680 A JP7944680 A JP 7944680A JP H0132435 B2 JPH0132435 B2 JP H0132435B2
- Authority
- JP
- Japan
- Prior art keywords
- air
- heat exchanger
- reversing heat
- hydrocarbons
- pipe
- 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
- 229930195733 hydrocarbon Natural products 0.000 claims description 45
- 150000002430 hydrocarbons Chemical class 0.000 claims description 45
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 33
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 22
- 230000008929 regeneration Effects 0.000 claims description 22
- 238000011069 regeneration method Methods 0.000 claims description 22
- 238000000034 method Methods 0.000 claims description 19
- 239000002912 waste gas Substances 0.000 claims description 19
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 16
- 239000001569 carbon dioxide Substances 0.000 claims description 16
- 239000007789 gas Substances 0.000 claims description 16
- 238000000926 separation method Methods 0.000 claims description 12
- 238000001179 sorption measurement Methods 0.000 claims description 12
- 239000003463 adsorbent Substances 0.000 claims description 10
- 238000000746 purification Methods 0.000 claims description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000002994 raw material Substances 0.000 claims description 5
- 230000001172 regenerating effect Effects 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 230000009467 reduction Effects 0.000 claims description 2
- 238000004821 distillation Methods 0.000 claims 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 25
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 18
- 239000007788 liquid Substances 0.000 description 15
- 239000004215 Carbon black (E152) Substances 0.000 description 11
- 229910001873 dinitrogen Inorganic materials 0.000 description 8
- 239000007791 liquid phase Substances 0.000 description 8
- 229910001882 dioxygen Inorganic materials 0.000 description 7
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 6
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 230000000694 effects Effects 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000000741 silica gel Substances 0.000 description 2
- 229910002027 silica gel Inorganic materials 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000000126 substance Substances 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
- F25J3/04248—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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04242—Cold end purification of the feed 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
- 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
- F25J2205/24—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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は空気液化分離装置における炭化水素の
除去方法に関し、詳しくはリバーシング熱交換器
を通過した原料空気を次いで吸着器に導入し、該
原料空気中に含有する炭化水素を除去することに
より精溜塔に到達する炭化水素を無くし、もつて
空気分離装置の安全性の向上と液体酸素放出によ
るロスの防止を図つた方法に関する。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to a method for removing hydrocarbons in an air liquefaction separation device. This invention relates to a method for eliminating hydrocarbons from reaching a rectification column by removing hydrocarbons contained in feed air, thereby improving the safety of an air separation device and preventing loss due to liquid oxygen release.
リバーシング熱交換器を用いて原料空気を冷却
する型式の空気液化分離装置においては、該リバ
ーシング熱交換器において原料空気に含有する水
分、炭酸ガスを凝結固化して析出除去し、該熱交
換器の原料空気流路に蓄積した水分、炭酸ガスは
原料空気流路と廃ガス流路とを交互に切換えるこ
とにより、昇華除去している。
In an air liquefaction separation device that uses a reversing heat exchanger to cool feed air, the reversing heat exchanger condenses and solidifies moisture and carbon dioxide contained in the feed air to precipitate and remove the heat exchanger. Moisture and carbon dioxide accumulated in the raw air flow path of the vessel are sublimated and removed by alternately switching between the raw air flow path and the waste gas flow path.
しかし、原料空気中の炭化水素類は、このリバ
ーシング熱交換器では除去されずに精溜塔に侵入
して液体空気、液体酸素中に濃縮されるので、低
温の液相吸着器により除去し、また常時一定量の
液体酸素を放出することにより安全を確保してい
る。 However, hydrocarbons in the feed air are not removed by this reversing heat exchanger but enter the rectification column and are concentrated in liquid air and liquid oxygen, so they are removed by a low-temperature liquid phase adsorber. Safety is also ensured by constantly releasing a certain amount of liquid oxygen.
例えば第１図に示すリバーシング熱交換器を使
用する全低圧式空気液化分離装置においては、次
の様な方法により、原料空気に同伴されて侵入す
る水分、炭酸ガス、炭化水素類を除去していた。 For example, in a total low-pressure air liquefaction separation device that uses a reversing heat exchanger as shown in Figure 1, the following method is used to remove moisture, carbon dioxide, and hydrocarbons that enter the feed air. was.
即ち、管１より導入された加圧原料空気は、切
換弁２ａ，２ｂ、管３ａ，３ｂ、リバーシング熱
交換器の温ブロツク４、冷ブロツク５のそれぞれ
の切換通路４ａ，４ｂ，５ａ，５ｂ、管６ａ，６
ｂ、戻止弁７ａ，７ｂからなる切換流路の一方、
例えば切換弁２ａ、管３ａ、切換通路４ａ，５
ａ、管６ａ、戻止弁７ａを通つて冷却されるとと
もに水分、炭酸ガスを除去されて管８に導出され
る。 That is, the pressurized raw air introduced from the pipe 1 is passed through the switching valves 2a, 2b, the pipes 3a, 3b, and the switching passages 4a, 4b, 5a, 5b of the hot block 4 and cold block 5 of the reversing heat exchanger, respectively. , tubes 6a, 6
b, one side of the switching flow path consisting of the return valves 7a and 7b;
For example, the switching valve 2a, the pipe 3a, the switching passages 4a, 5
a, a pipe 6a, and a check valve 7a, where it is cooled, moisture and carbon dioxide are removed, and the water is led out to a pipe 8.
尚、上記リバーシング熱交換器の温ブロツク４
及び冷ブロツク５には、それぞれ酸素ガス通路４
ｃ，５ｃ、窒素ガス通路４ｄ，５ｄが設けられる
とともに、冷ブロツク５には再熱回路５ｅが設け
られている。 In addition, the heating block 4 of the reversing heat exchanger
and the cold block 5 are each provided with an oxygen gas passage 4.
In addition, the cold block 5 is provided with a reheat circuit 5e.
前記管８に導出した原料空気は、一部を管１６
に分岐した後、大部分が管９を経て精溜塔の下部
塔１０に導入されて精溜され、下部塔１０上部に
生成した液体窒素は、弁１５を経て上部塔１３に
導入される。 A portion of the raw air led out to the pipe 8 is passed through the pipe 16.
After branching, most of the liquid nitrogen is introduced into the lower column 10 of the rectification column via pipe 9 to be rectified, and the liquid nitrogen generated above the lower column 10 is introduced into the upper column 13 via valve 15.
また、管８から管１６に分岐した原料空気の一
部は、リバーシング熱交換器の冷ブロツク５の再
熱回路５ｅを経た後、管１７から膨脹タービン１
８に導入され、降圧して管１９から精溜塔の上部
塔１３に導入される。この時前記リバーシング熱
交換器で捕足されなかつた微量の炭化水素類は上
部塔１３に侵入する。 A part of the feed air branched from the pipe 8 to the pipe 16 passes through the reheat circuit 5e of the cold block 5 of the reversing heat exchanger, and then flows from the pipe 17 to the expansion turbine 1.
8, the pressure is reduced, and the product is introduced into the upper column 13 of the rectification column through a pipe 19. At this time, trace amounts of hydrocarbons not captured by the reversing heat exchanger enter the upper column 13.
下部塔１０底部の液体空気は、炭化水素吸着器
１４によつて含有する炭化水素の大部分を除去さ
れて弁１２を経て上部塔１３に導入される。 The liquid air at the bottom of the lower column 10 is introduced into the upper column 13 through the valve 12 after most of the hydrocarbons contained therein are removed by the hydrocarbon adsorber 14 .
また、上部塔１３下部の凝縮器１１に溜る液体
酸素は、液酸ポンプ２０で循環し、循環吸着器２
１により液体酸素中の炭化水素を濾過し、液相中
のアセチレン等を捕捉する。しかし、この液相に
含有するメタンは、循環吸着器２１では殆んど濾
過せず通過し、前記膨脹タービン１８の経路から
の炭化水素と共に液体酸素中に蓄積されて行き、
次第に高濃度になつて行くので、常時一定量の液
体酸素を管２２より装置外へ放出して安全を確保
している。 In addition, the liquid oxygen accumulated in the condenser 11 at the bottom of the upper column 13 is circulated by the liquid acid pump 20, and
1 to filter hydrocarbons in liquid oxygen and capture acetylene, etc. in the liquid phase. However, the methane contained in this liquid phase passes through the circulation adsorber 21 without being filtered, and is accumulated in the liquid oxygen together with the hydrocarbons from the path of the expansion turbine 18.
Since the concentration gradually increases, a certain amount of liquid oxygen is always released from the pipe 22 to the outside of the device to ensure safety.
尚、精溜塔の凝縮器１１から導出する製品酸素
ガスは、管２３、上記酸素ガス通路５ｃ，４ｃを
経て管３１から採取される。また、精溜塔の上部
塔１３から導出する純窒素ガスは、管２４、上記
純窒素ガス通路５ｄ，４ｄを経て管３２から採取
され、上部塔１３の不純窒素、即ち廃ガスは、管
２５、弁２６、管２７を経た後に上記切換流路の
一方に帰還し、例えば戻止弁７ｂ、管６ｂ、切換
通路５ｂ，４ｂ、管３ｂ、切換弁２ｂを経て切換
通路５ｂ，４ｂに析出した水分、炭酸ガスを昇華
同伴して管２８、制動用ブロワー２９，管３０を
経て放出される。 Note that the product oxygen gas led out from the condenser 11 of the rectification column is collected from the pipe 31 via the pipe 23 and the oxygen gas passages 5c and 4c. Further, pure nitrogen gas led out from the upper column 13 of the rectification column is collected from the pipe 32 via the pipe 24 and the pure nitrogen gas passages 5d and 4d, and impure nitrogen from the upper column 13, that is, waste gas, is collected from the pipe 25. , the valve 26, and the pipe 27, and then returned to one of the switching passages, and deposited in the switching passages 5b, 4b, for example, via the check valve 7b, the pipe 6b, the switching passages 5b, 4b, the pipe 3b, and the switching valve 2b. Moisture and carbon dioxide are sublimed and entrained and discharged through the pipe 28, the brake blower 29, and the pipe 30.
しかし、前述のごとく、下部塔１０底部の液体
空気は、弁１２を経て上部塔１３に導入される際
に、炭化水素吸着器１４によつて液体空気中に含
有する炭化水素を除去されるが、炭化水素吸着器
１４で除去されるのは、主としてアセチレンであ
り、メタンは捕捉されずに上部塔１３に侵入す
る。したがつて、前記膨脹タービン１８を経て来
る経路及び炭化水素吸着器１４を経て来る経路の
双方から上部塔１３に侵入した炭化水素類は、上
部塔１３下部の凝縮器１１に溜る液体酸素中に濃
縮される。
However, as described above, when the liquid air at the bottom of the lower column 10 is introduced into the upper column 13 through the valve 12, the hydrocarbons contained in the liquid air are removed by the hydrocarbon adsorber 14. , it is mainly acetylene that is removed in the hydrocarbon adsorber 14, and methane enters the upper column 13 without being captured. Therefore, the hydrocarbons that have entered the upper column 13 from both the path passing through the expansion turbine 18 and the path passing through the hydrocarbon adsorber 14 are contained in the liquid oxygen accumulated in the condenser 11 at the bottom of the upper column 13. Concentrated.
そこで前述の如く、液酸ポンプ２０により、こ
の液体酸素を循環し、循環吸着器２１により液体
酸素中の炭化水素を濾過しているが、ここでも液
相中のメタンは殆んど通過し、アセチレン等が捕
捉される。したがつて、メタンは液体酸素中に蓄
積されて行き、次第に高濃度になつて行くので常
時一定量の液体酸素を管２２より装置外へ放出す
ることにより、危険な状態になるのを防いでい
る。 Therefore, as mentioned above, this liquid oxygen is circulated by the liquid acid pump 20, and the hydrocarbons in the liquid oxygen are filtered by the circulation adsorber 21, but here too, most of the methane in the liquid phase passes through. Acetylene etc. are captured. Therefore, methane accumulates in the liquid oxygen and gradually becomes highly concentrated, so a dangerous situation can be prevented by constantly releasing a certain amount of liquid oxygen to the outside of the device through the pipe 22. There is.
このため上記従来法では製品となる液体酸素の
ロス及び寒冷のロスを避けられなかつた。 For this reason, in the conventional method described above, loss of liquid oxygen and loss of cooling cannot be avoided.
また上記炭化水素吸着器１４及び循環吸着器２
１は、吸着した炭化水素を脱着し、再生しなけれ
ば連続使用できないので、両吸着器１４，２１を
それぞれ複数設けて切換え使用し、しかもこれら
の両吸着器１４，２１を再生するためには、別途
再生用ガスの供給源と該再生用ガスを加熱するた
めの加熱源を必要としていた。 In addition, the hydrocarbon adsorption device 14 and the circulation adsorption device 2
1 cannot be used continuously unless the adsorbed hydrocarbons are desorbed and regenerated, so a plurality of both adsorbers 14 and 21 are provided and used selectively, and in order to regenerate both adsorbers 14 and 21, , a separate supply source for regeneration gas and a heating source for heating the regeneration gas were required.
そこで、本発明は、リバーシング熱交換器がプ
レツシヤ−スイング操作されていることに着目
し、リバーシング熱交換器の直後に吸着器を設
け、リバーシング熱交換器の切換に同期して該吸
着器を切換えて炭化水素類を除去するようにし、
液体酸素及びその寒冷のロスや吸着器再生のため
の熱損失を解消した空気分離装置における炭化水
素の除去方法を提供することを目的としている。 Therefore, the present invention focuses on the fact that the reversing heat exchanger is operated under pressure swing, and an adsorber is provided immediately after the reversing heat exchanger, and the adsorption device is installed in synchronization with the switching of the reversing heat exchanger. Change the equipment to remove hydrocarbons,
The object of the present invention is to provide a method for removing hydrocarbons in an air separation device that eliminates the loss of liquid oxygen and its refrigeration and the heat loss for adsorber regeneration.
本発明方法は、原料空気をリバーシング熱交換
器に導入して冷却し、同時に含有する水分及び炭
酸ガスを析出させて除去した後、吸着剤を充填し
切換使用する吸着器に導入して、該低温原料空気
中に含有する炭化水素類を吸着除去する精製工程
と、精溜塔より帰還する廃ガスを前記吸着器に導
入して上記精製工程で前記吸着剤中に吸着された
炭化水素類を脱着した後、上記リバーシング熱交
換器に導入して上記精製工程で析出した水分及び
炭酸ガスを同伴して該リバーシング熱交換器を再
生する再生工程とを有し、前記精製工程と再生工
程を、リバーシング熱交換器の切換周期と同周期
に切換えることを特徴としている。
In the method of the present invention, raw air is introduced into a reversing heat exchanger to be cooled, and at the same time, moisture and carbon dioxide contained therein are precipitated and removed, and then an adsorbent is filled and introduced into an adsorber that is switched to use. A purification step in which hydrocarbons contained in the low-temperature feed air are adsorbed and removed, and waste gas returned from a rectification tower is introduced into the adsorber to produce hydrocarbons adsorbed in the adsorbent in the purification step. and a regeneration step of regenerating the reversing heat exchanger by introducing it into the reversing heat exchanger and entraining the moisture and carbon dioxide precipitated in the refining step, and regenerating the reversing heat exchanger. It is characterized by switching the process at the same cycle as the switching cycle of the reversing heat exchanger.
また製品酸素及び製品窒素の採取率が高く、リ
バーシング熱交換器の非切換通路（酸素ガス通
路、窒素ガス通路）に不純物の混入が許されない
これら製品ガスを大量に流す場合には、原料空気
に対する廃ガスの比率が低くなり、したがつて炭
化水素吸着器の再生が困難となるが、この場合は
真空ポンプによつて廃ガスを大気圧以下の圧力に
減圧排気することにより、吸着器の再生を行なう
ことも含むものである。 In addition, when the extraction rate of product oxygen and product nitrogen is high and a large amount of these product gases, which do not allow impurities to be mixed into the non-switching passages (oxygen gas passage, nitrogen gas passage) of the reversing heat exchanger, are flowing, it is necessary to The ratio of the waste gas to the hydrocarbon adsorber becomes low, making it difficult to regenerate the hydrocarbon adsorber. This also includes regeneration.
さらに上記廃ガスの減圧排気による吸着器の再
生工程の減圧を膨脹タービンの制動用ブロワーに
よつて行なうことも含むものである。 Furthermore, the present invention also includes the use of a brake blower of the expansion turbine to reduce the pressure in the adsorber regeneration step by exhausting the waste gas under reduced pressure.
上記のごとく構成することにより、原料空気が
液化して精溜塔に導入される前に、低温圧力スイ
ング吸着方法により不純物である炭化水素類を除
去でき、空気分離装置の安全性の向上と液体酸素
放出による製品のロス及び寒冷のロスを防止する
ことができる。
With the above configuration, impurities such as hydrocarbons can be removed using the low temperature pressure swing adsorption method before the feed air is liquefied and introduced into the rectification column, improving the safety of the air separation equipment and Product loss and cold loss due to oxygen release can be prevented.
また、リバーシング熱交換器は、数分から数十
分の短時間で切換えられているため、吸着器も同
じ短時間での切換となり、吸着剤の量を少なくす
ることができる。しかも、吸着器の再生は、リバ
ーシング熱交換器の再生を行うための低温低圧の
廃ガスをそのまま用いるので、別途再生用ガスを
用意する必要がなく、再生用ガスの供給源や加熱
源を必要としない。 Further, since the reversing heat exchanger is switched in a short time of several minutes to several tens of minutes, the adsorbent can also be switched in the same short time, and the amount of adsorbent can be reduced. Moreover, the regeneration of the adsorber uses the low-temperature, low-pressure waste gas that is used to regenerate the reversing heat exchanger, so there is no need to prepare a separate regeneration gas, and the regeneration gas supply source and heating source are not required. do not need.
以下本発明を第２図に示す一実施例にしたがつ
て説明する。尚、本実施例は、吸着器の再生工程
の減圧を膨脹タービンの制動用ブロワーによつて
行なう場合の例である。また前記第１図に示した
従来例と同一要素のものには同一符号を付して詳
細な説明を省略する。
The present invention will be described below with reference to an embodiment shown in FIG. Note that this embodiment is an example in which the pressure reduction in the regeneration process of the adsorber is performed by a brake blower of an expansion turbine. Further, the same elements as those of the conventional example shown in FIG. 1 are given the same reference numerals and detailed explanations will be omitted.
管１より6ata、30℃の原料空気10000Nm3／ｈ
が導入され、一方の切換弁２ａ、管３ａを経てリ
バーシング熱交換器の温ブロツク４の切換通路４
ａを流れて冷却されると共にその伝熱面に水分を
凝結させ、さらにリバーシング熱交換器の冷ブロ
ツク５の切換通路５ａを流れて−170℃まで冷却
され、その伝熱面に炭酸ガスを析出させると共に
自身は精製されて管６ａより導出する。 6ata, 30℃ raw air 10000Nm 3 /h from pipe 1
is introduced into the switching passage 4 of the hot block 4 of the reversing heat exchanger via one switching valve 2a and the pipe 3a.
It flows through the switching passage 5a of the cold block 5 of the reversing heat exchanger and is cooled to -170°C, and carbon dioxide gas is condensed on the heat transfer surface of the reversing heat exchanger. At the same time as it is precipitated, it is purified and discharged from the tube 6a.
この管６ａを導出した低温空気には、原料空気
と同濃度のメタン１〜2ppm及び極微量のアセチ
レン等が含まれるが、これらの炭化水素類を除去
するために、該低温空気は次いでシリカゲル等の
吸着剤を充填し、切換使用される一対でなる吸着
器３３ａ，３３ｂの一方の吸着器３３ａに導入さ
れ、炭化水素類が吸着除去される。これらのリバ
ーシング熱交換器による水分、炭酸ガスの析出除
去、及び吸着器による炭化水素類の吸着除去から
なる精製工程により含有不純物を完全に除去され
た精製低温空気は戻止弁７ａを経て管８へ導出さ
れる。 The low-temperature air led out of this tube 6a contains 1 to 2 ppm of methane at the same concentration as the raw air, and a trace amount of acetylene, etc., but in order to remove these hydrocarbons, the low-temperature air is then treated with silica gel, etc. The adsorbent is introduced into one adsorber 33a of a pair of adsorbers 33a and 33b which are used alternately, and hydrocarbons are adsorbed and removed. Purified low-temperature air from which impurities have been completely removed through a purification process consisting of precipitation and removal of moisture and carbon dioxide by these reversing heat exchangers, and adsorption and removal of hydrocarbons by an adsorption device, is passed through a return valve 7a into a pipe. 8.
ここで、前記切換弁２ａ，２ｂ及び戻止弁７
ａ，７ｂは、リバーシング熱交換器の切換通路４
ａ，４ｂ，５ａ，５ｂ、さらに吸着器３３ａ，３
３ｂを夫々切換えるためのものであり、５〜10分
の間隔で作動し、これにより各通路及び各吸着器
を原料空気と廃ガスが交替して流れる。即ち上記
説明では、それぞれ符号にａを付した通路に原料
空気が流れ、含有する水分、炭酸ガス、炭化水素
類を除去される精製工程を行つており、同じくｂ
を付した通路に帰還した廃ガスが流れ、後述の再
生工程を行つている状態である。 Here, the switching valves 2a, 2b and the return valve 7
a, 7b are switching passages 4 of the reversing heat exchanger
a, 4b, 5a, 5b, and further adsorbers 33a, 3
3b, and are operated at intervals of 5 to 10 minutes, so that feed air and waste gas alternately flow through each passage and each adsorber. That is, in the above explanation, the raw air flows through the passages marked with a, and a purification process is carried out in which the contained moisture, carbon dioxide gas, and hydrocarbons are removed, and similarly, b
The returned waste gas flows through the passage marked with , undergoing the regeneration process described below.
管８へ導出した精製低温空気は二分され、その
第１の流れ8000Nm3／ｈは管９を経て複式精溜塔
の下部塔１０に供給され、ここで凝縮器１１によ
る上昇ガスの凝縮液化、液体空気の還流作用によ
つて精溜が行なわれ、下部の酸素富化液体空気と
上部の液体窒素に分離し、該酸素富化液体空気
は、弁１２を経て膨脹し、温度降下して上部塔１
３に導入されさらに精溜に供される。 The purified low-temperature air led out to pipe 8 is divided into two parts, and the first stream of 8000 Nm 3 /h is fed via pipe 9 to the lower column 10 of the double rectification column, where the rising gas is condensed and liquefied by a condenser 11. Rectification is performed by the reflux action of the liquid air, separating it into oxygen-enriched liquid air in the lower part and liquid nitrogen in the upper part. Tower 1
3 and further subjected to rectification.
この場合、前記従来法では、この経路に炭化水
素吸着器１４が挿入されていたが、本発明方法に
よる場合は前記吸着器３３ａで除去されているた
め、その必要が無い。 In this case, in the conventional method, the hydrocarbon adsorber 14 was inserted into this path, but in the method of the present invention, since the hydrocarbon adsorber 33a removes the hydrocarbons, this is not necessary.
また下部塔１０上部に溜つた液体窒素は、弁１
５を経て上部塔１３の上部へ送られ上部塔１３の
還流液となる。 In addition, the liquid nitrogen accumulated in the upper part of the lower column 10 is removed from the valve 1
5 and is sent to the upper part of the upper column 13 and becomes the reflux liquid of the upper column 13.
一方、前記管１６に分岐した精製低温空気の第
２の流れ2000Nm3／ｈは、管１６を経てリバーシ
ング熱交換器５の再熱通路５ｅに導入され、昇温
して−130℃、5.6ataとなつて導出し、管１７を
経て膨脹タービン１８に入り、ここで断熱膨脹し
て−170℃、1.3ataの状態で管１９より上部塔１
３に導入される。 On the other hand, the second flow of 2000 Nm 3 /h of purified low-temperature air branched into the pipe 16 is introduced into the reheat passage 5e of the reversing heat exchanger 5 through the pipe 16, and is heated to -130°C, 5.6 It enters the expansion turbine 18 through the pipe 17, where it is adiabatically expanded and then passed through the pipe 19 to the upper tower 1 at -170°C and 1.3 ata.
3 will be introduced.
この様にして上部塔１３に導入された各液及び
ガスは、精溜によつて分離され、上部塔１３下部
の凝縮器１１には製品液体酸素が、上部塔１３上
部には窒素ガスが集まる。 The liquids and gases introduced into the upper column 13 in this way are separated by rectification, and product liquid oxygen is collected in the condenser 11 at the bottom of the upper column 13, and nitrogen gas is collected in the upper part of the upper column 13. .
凝縮器１１に溜つた液体酸素は、従来は前記の
如く、液酸ポンプ２０により循環し、循環吸着器
２１による吸着除去、そして管２２よりの放出に
よつて、濃縮された炭化水素類を除いていたが、
本発明方法によれば、この様な装置及び操作は必
要ない。 Conventionally, as described above, the liquid oxygen accumulated in the condenser 11 is circulated by the liquid acid pump 20, adsorbed and removed by the circulation adsorber 21, and then discharged from the pipe 22 to remove concentrated hydrocarbons. was, but
According to the method of the invention, such equipment and operations are not required.
この様にして分離された空気の各成分は、管２
３より酸素ガス1500Nm3／ｈが、管２４より純窒
素ガス3500Nm3／ｈが、また管２５より不純窒素
ガス、即ち廃ガス5000Nm3／ｈが導出される。 Each component of the air separated in this way is
3, 1500 Nm 3 /h of oxygen gas is led out, 3500 Nm 3 /h of pure nitrogen gas is led out from pipe 24, and 5000 Nm 3 /h of impure nitrogen gas, that is, waste gas, is led out from pipe 25.
この廃ガスは、弁２６により1.3ataから
0.95ataに膨脹し、管２７、戻止弁７ｂを経て吸
着器３３ｂに導入され、該吸着器３３ｂ内のシリ
カゲル等の吸着剤に吸着されているメタン、アセ
チレン等の炭化水素類を脱着同伴してこれを再生
し、さらに管６ｂを経てリバーシング熱交換器の
冷ブロツク５の切換通路５ｂ及び温ブロツク４の
切換通路４ｂを通り、切換通路５ｂ，４ｂの伝熱
面に前周期において凝結し析出している炭酸ガス
及び水分を気化し同伴してこれら切換通路５ｂ，
４ｂを再生し、自身は常温迄昇温して導出し、こ
れらの吸着器３３ｂの炭化水素類の脱着及びリバ
ーシング熱交換器の炭酸ガス、水分の気化からな
る再生工程を終えた廃ガスは、管３ｂ、切換弁２
ｂを経て管２８に至る。この廃ガスは管２８より
さらに膨脹タービン１８の制動用ブロワー２９に
入り0.85ataから1ataまで圧縮されて管３０より
装置外へ排出される。 This waste gas is removed from 1.3 ata by valve 26.
It expands to 0.95 ata and is introduced into the adsorber 33b through the pipe 27 and the return valve 7b, where it desorbs and entrains hydrocarbons such as methane and acetylene adsorbed on the adsorbent such as silica gel in the adsorber 33b. This is regenerated, and further passes through the switching passage 5b of the cold block 5 and the switching passage 4b of the hot block 4 of the reversing heat exchanger via the pipe 6b, and condenses on the heat transfer surfaces of the switching passages 5b and 4b in the previous cycle. The precipitated carbon dioxide and moisture are vaporized and entrained to these switching passages 5b,
4b is regenerated, the waste gas itself is heated to room temperature and extracted, and the waste gas that has completed the regeneration process consisting of desorption of hydrocarbons in the adsorber 33b and vaporization of carbon dioxide and moisture in the reversing heat exchanger is , pipe 3b, switching valve 2
It reaches the pipe 28 via b. This waste gas further enters the brake blower 29 of the expansion turbine 18 through the pipe 28, is compressed from 0.85 ata to 1 ata, and is discharged from the apparatus through the pipe 30.
上記制動用ブロワー２９は、排ガスを吸引して
弁２６から下流、即ち管２７、戻止弁７ｂ、吸着
器３３ｂ、リバーシング熱交換器の切換通路５
ｂ，４ｂ、切換弁２ｂ、管２８に至る経路を減圧
状態とするもので、制動用ブロワー２９の代りに
通常の真空ポンプを使用することにより、管２
７、戻止弁７ｂ、吸着器３３ｂ、リバーシング熱
交換器の切換通路５ｂ，４ｂ、切換弁２ｂ、管２
８に至る経路を減圧しても良いことは勿論であ
る。 The brake blower 29 sucks the exhaust gas and operates downstream from the valve 26, that is, the pipe 27, the return valve 7b, the adsorber 33b, and the switching passage 5 of the reversing heat exchanger.
b, 4b, the switching valve 2b, and the pipe 28 are reduced in pressure, and by using a normal vacuum pump instead of the brake blower 29, the pipe 2
7, return valve 7b, adsorber 33b, reversing heat exchanger switching passages 5b, 4b, switching valve 2b, pipe 2
Of course, the pressure may be reduced on the path leading to No. 8.
一方、管２３より導出された酸素ガスは、リバ
ーシング熱交換器の酸素ガス通路５ｃ，４ｃを通
り、向流する原料空気を冷却し、自身は常温迄昇
温して管３１より製品として取出される。また管
２４より導出した純窒素ガスは、リバーシング熱
交換器の窒素ガス通路５ｄ，４ｄを通り、同様に
向流する原料空気を冷却し、自身は常温迄昇温し
て管３２より製品として取り出される。 On the other hand, the oxygen gas led out from the pipe 23 passes through the oxygen gas passages 5c and 4c of the reversing heat exchanger, cools the countercurrent raw material air, heats itself to room temperature, and takes it out as a product from the pipe 31. be done. In addition, the pure nitrogen gas led out from the pipe 24 passes through the nitrogen gas passages 5d and 4d of the reversing heat exchanger, cools the raw material air flowing countercurrently, and heats itself to room temperature, and then passes through the pipe 32 as a product. taken out.
そして、前記切換弁２ａ，２ｂ及び戻止弁７
ａ，７ｂが所定の時間間隔で切換作動し、これに
よりリバーシング熱交換器の各切換通路４ａ，４
ｂ，５ａ，５ｂ及び各吸着器３３ａ，３３ｂを流
れる原料空気と廃ガスが交替して、即ち上記説明
とは逆に、それぞれ符号にａを付した通路に帰還
した廃ガスが流れて再生工程を行い、同じくｂを
付した通路に原料空気が流れ、含有する水分、炭
酸ガス、炭化水素類を除去される精製工程を行う
状態に切換えられる。これにより、吸着器３３
ａ，３３ｂの切換とリバーシング熱交換器の切換
通路４ａ，４ｂ，５ａ，５ｂの切換が同周期に行
われることになる。 Then, the switching valves 2a, 2b and the return valve 7
a, 7b are switched at predetermined time intervals, thereby each switching passage 4a, 4 of the reversing heat exchanger
b, 5a, 5b and the respective adsorbers 33a, 33b, the raw material air and waste gas are exchanged, that is, contrary to the above explanation, the returned waste gas flows into the passages marked with a, respectively, and a regeneration process is performed. Then, the feed air flows through the passage marked b, and the state is switched to a state in which a purification process is performed in which the contained moisture, carbon dioxide gas, and hydrocarbons are removed. As a result, the adsorber 33
Switching of channels a and 33b and switching of switching passages 4a, 4b, 5a and 5b of the reversing heat exchanger are performed in the same period.
したがつて、吸着器３３ａ，３３ｂは、低温高
圧の原料空気が流れる精製工程と、低温低圧の廃
ガスが流れる再生工程とを、リバーシング熱交換
器の切換通路４ａ，４ｂ，５ａ，５ｂの切換を行
う切換弁２ａ，２ｂ及び戻止弁７ａ，７ｂの作動
で行うことができるので、加熱再生ガスの供給及
び切換弁等の再生用の設備を用意する必要がな
く、吸着設備の付加のみで良い。 Therefore, the adsorbers 33a and 33b perform a purification process in which low-temperature, high-pressure raw material air flows and a regeneration process in which low-temperature, low-pressure waste gas flows through switching passages 4a, 4b, 5a, and 5b of the reversing heat exchanger. Since switching can be performed by operating the switching valves 2a, 2b and check valves 7a, 7b, there is no need to supply heated regeneration gas or prepare regeneration equipment such as switching valves, and only add adsorption equipment. That's fine.
本発明は以上の如く実施されるが、これによる
効果は次の通りである。
The present invention is carried out as described above, and the effects thereof are as follows.
従来、液相において除去していたメタン、アセ
チレン等の炭化水素類をリバーシング熱交換器で
水分及び炭酸ガスを除去された精製空気を直ちに
吸着器に導入して気相において吸着除去するよう
にしたから、液相において吸着除去し得なかつた
メタンも吸着除去し得る様になり、従来必要とし
た液相での炭化水素吸着器や循環吸着器が不要に
なつただけでなく、酸素と共存すると極めて危険
な挙動を起こす上記物質が凝縮器の液体酸素中に
濃縮されることが無くなつたので、保安上非常に
好ましい結果が得られる様になつた。また、酸素
中に炭化水素が濃縮されるのを防ぐための、定常
的な液体酸素の放出が不要になつたから、製品の
ロス及びそれによる寒冷のロスが防止できる様に
なり、経済的にもメリツトが生じる様になつた。 Hydrocarbons such as methane and acetylene, which were conventionally removed in the liquid phase, are removed by adsorption in the gas phase by immediately introducing purified air from which water and carbon dioxide have been removed in a reversing heat exchanger into an adsorbent. As a result, methane, which could not be adsorbed and removed in the liquid phase, can now be adsorbed and removed, which not only eliminates the need for hydrocarbon adsorbers and circulation adsorbers in the liquid phase that were previously required, but also eliminates the need for methane that coexists with oxygen. As a result, the above-mentioned substances that cause extremely dangerous behavior are no longer concentrated in the liquid oxygen in the condenser, so very favorable results can be obtained in terms of safety. In addition, since there is no longer a need for constant discharge of liquid oxygen to prevent hydrocarbons from concentrating in oxygen, product loss and resulting loss of cooling can be prevented, making it economically viable. Benefits began to emerge.
さらに、吸着器の再生をリバーシング熱交換器
の再生と同周期に行い、リバーシング熱交換器の
再生に使用される低温低圧の廃ガスを、そのまま
用いているので、別途再生用ガス等を用意する必
要がなく、再生用ガスの供給源や加熱源を必要と
せず、しかも液相での炭化水素吸着器、循環吸着
器が不要となつたので、これらの加熱再生に要す
る費用も不要となる。 Furthermore, the adsorber is regenerated in the same cycle as the reversing heat exchanger, and the low-temperature, low-pressure waste gas used to regenerate the reversing heat exchanger is used as is, so a separate regeneration gas, etc. is used. There is no need to prepare a regeneration gas supply source or heating source, and there is no need for a liquid phase hydrocarbon adsorption device or circulation adsorption device, so there is no need to pay for these heating regeneration costs. Become.
また、リバーシング熱交換器を導出した低温原
料空気に極微量含まれる雪状のドライアイスも、
本発明方法による吸着器により捕集除去し得る副
次的効果もある。 In addition, the snow-like dry ice contained in extremely small amounts in the low-temperature raw air from which the reversing heat exchanger was derived,
There are also side effects that can be collected and removed by the adsorber according to the method of the invention.
加えて、本発明は、リバーシング熱交換器と戻
止弁との間に吸着器を配置するだけで実施するこ
とができ、建設コストも掛らず、従来装置にも容
易に適用することが可能である。 In addition, the present invention can be implemented by simply arranging an adsorber between the reversing heat exchanger and the check valve, requires no construction cost, and can be easily applied to conventional equipment. It is possible.
第１図は従来の空気分離装置の系統図、第２図
は本発明の除去方法を適用した空気分離装置の系
統図である。
２ａ，２ｂ……切換弁、４……リバーシング熱
交換器の温ブロツク、５……リバーシング熱交換
器の冷ブロツク、７ａ，７ｂ……戻止弁、１０…
…複式精溜塔の下部塔、１１……凝縮器、１３…
…複式精溜塔の上部塔、１８……膨脹タービン、
２９……制動用ブロワー、３３ａ，３３ｂ……吸
着器。
FIG. 1 is a system diagram of a conventional air separation device, and FIG. 2 is a system diagram of an air separation device to which the removal method of the present invention is applied. 2a, 2b...Switching valve, 4...Hot block of reversing heat exchanger, 5...Cold block of reversing heat exchanger, 7a, 7b...Return valve, 10...
...Lower column of double rectification column, 11... Condenser, 13...
...upper column of a double rectification column, 18...expansion turbine,
29... Braking blower, 33a, 33b... Adsorption device.
Claims (1)
冷却及び精製した後、精溜塔に導いて酸素・窒素
を採取する空気液化分離装置において、原料空気
を上記リバーシング熱交換器に導入して冷却し、
同時に含有する水分及び炭酸ガスを析出させて除
去した後、吸着剤を充填し切換使用する吸着器に
導入して、該低温原料空気中に含有する炭化水素
類を吸着除去する精製工程と、精溜塔より帰還す
る廃ガスを前記吸着器に導入して上記精製工程で
前記吸着剤中に吸着された炭化水素類を脱着した
後、上記リバーシング熱交換器に導入して上記精
製工程で析出した水分及び炭酸ガスを同伴して該
リバーシング熱交換器を再生する再生工程とを有
し、前記精製工程と再生工程を、リバーシング熱
交換器の切換周期と同周期に切換えることを特徴
とする空気分離装置における炭化水素の除去方
法。 ２ 上記廃ガスによる前記吸着剤の再生工程を減
圧下で行なう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炭化水素の除去
方法。 ３ 上記減圧下で行う再生工程の減圧を、膨張タ
ービンの制動用ブロワーにより行なうことを特徴
とする特許請求の範囲第２項記載の空気分離装置
における炭化水素の除去方法。[Claims] 1. In an air liquefaction separation device that cools and refines feed air using a reversing heat exchanger and then leads it to a rectification column to extract oxygen and nitrogen, the feed air is heated by the reversing heat. Introduced into the exchanger and cooled,
At the same time, the water and carbon dioxide contained in the air are precipitated and removed, and then an adsorbent is filled and introduced into a switchable adsorption device to adsorb and remove hydrocarbons contained in the low-temperature raw material air. The waste gas returned from the distillation column is introduced into the adsorber to desorb the hydrocarbons adsorbed in the adsorbent in the purification process, and then introduced into the reversing heat exchanger to be precipitated in the purification process. and a regeneration step of regenerating the reversing heat exchanger by entraining the water and carbon dioxide gas, and the purification step and the regeneration step are switched at the same cycle as the switching cycle of the reversing heat exchanger. A method for removing hydrocarbons in air separation equipment. 2. The method for removing hydrocarbons in an air separation apparatus according to claim 1, wherein the step of regenerating the adsorbent using the waste gas is performed under reduced pressure. 3. The method for removing hydrocarbons in an air separation apparatus according to claim 2, wherein the pressure reduction in the regeneration step performed under reduced pressure is performed by a brake blower of an expansion turbine.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7944680A JPS576281A (en) | 1980-06-12 | 1980-06-12 | Carbon dioxide removal of air separator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7944680A JPS576281A (en) | 1980-06-12 | 1980-06-12 | Carbon dioxide removal of air separator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS576281A JPS576281A (en) | 1982-01-13 |
| JPH0132435B2 true JPH0132435B2 (en) | 1989-06-30 |
Family
ID=13690100
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7944680A Granted JPS576281A (en) | 1980-06-12 | 1980-06-12 | Carbon dioxide removal of air separator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS576281A (en) |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5337585A (en) * | 1976-09-21 | 1978-04-06 | Nippon Oxygen Co Ltd | Air separation method by adsorption |
-
1980
- 1980-06-12 JP JP7944680A patent/JPS576281A/en active Granted
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5337585A (en) * | 1976-09-21 | 1978-04-06 | Nippon Oxygen Co Ltd | Air separation method by adsorption |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS576281A (en) | 1982-01-13 |
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