JPH0131116B2 - - Google Patents
Info
- Publication number
- JPH0131116B2 JPH0131116B2 JP58128000A JP12800083A JPH0131116B2 JP H0131116 B2 JPH0131116 B2 JP H0131116B2 JP 58128000 A JP58128000 A JP 58128000A JP 12800083 A JP12800083 A JP 12800083A JP H0131116 B2 JPH0131116 B2 JP H0131116B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- liquefied
- product
- product gas
- 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
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
- F25J3/04472—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
- F25J3/04496—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
- F25J3/04503—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist by exchanging "cold" between at least two different cryogenic liquids, e.g. independently from the main heat exchange line of the air fractionation and/or by using external alternating storage systems
-
- 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
- F25J3/0409—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 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
- 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
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
- F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
-
- 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
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
-
- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/50—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being 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
- F25J2250/42—One fluid being nitrogen
-
- 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
- F25J2250/50—One fluid being 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
- 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)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
【発明の詳細な説明】
本発明は一般的なガス製造装置によつて製出さ
れる製品ガスの製造量と需要先の使用量とがバラ
ンスしない場合の経済的な対策を提供する、製品
ガス使用量の変動に追随可能なガス液化及び気化
方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention provides an economical solution for the case where the amount of product gas produced by a general gas production device and the amount used by a consumer are not balanced. This invention relates to a gas liquefaction and vaporization method that can follow changes in quantity.
例えば、配管で使用先と連結したガス製造装置
では、使用量が変動した場合の対策として最も簡
単な手段は、配管途中にガスホルダーを設けるこ
とである。しかし、かゝる手段ではガスホルダー
の容積以上の変動には対処することができない。 For example, in a gas production device connected to a user via piping, the simplest measure against fluctuations in usage is to install a gas holder in the middle of the piping. However, such means cannot cope with fluctuations greater than the volume of the gas holder.
次に考えられるのは、製品の一部を液体（低温
液化ガス）として取り出せる装置として、この製
品液体をタンクに貯留しておき、使用量が製品ガ
スの製出量を上回るときは、該製品液体をタンク
から取り出して蒸発器で気化させ、このガスを使
用先へ送ることである。しかしながら、製品を液
体で取り出すためにはそれだけ多くのエネルギー
（電力）を消費する必要があるが、この方式では
このエネルギーを回収することなく、単に気化し
て使用すると言う欠点がある。 The next possibility is to use a device that can extract part of the product as a liquid (low-temperature liquefied gas) and store this product liquid in a tank, and if the amount used exceeds the production amount of product gas, the product The process involves removing liquid from a tank, vaporizing it in an evaporator, and sending the gas to its intended use. However, it is necessary to consume a lot of energy (power) to extract the product in liquid form, but this method has the disadvantage that this energy is simply vaporized and used without being recovered.
本発明者等は、前述のような無駄なエネルギー
を消費することなく、冷媒の寒冷と寒冷サイクル
を有効に利用して、製品ガス使用量の変動に追随
し得る空気液化分離方法の開発に成功したもので
あり、本発明方法の技術的構成は前記特許請求の
範囲に明記したとおりであるが、本発明方法の一
例として、ガス製造装置が空気分離装置である場
合のフローシートを示す添付図面に基いて詳述す
る。 The present inventors have succeeded in developing an air liquefaction separation method that can follow fluctuations in product gas consumption by effectively utilizing the cooling of the refrigerant and the cooling cycle without consuming wasted energy as described above. The technical configuration of the method of the present invention is as specified in the claims, but as an example of the method of the present invention, the attached drawings show a flow sheet when the gas production device is an air separation device. The details will be explained based on the following.
図面において、空気分離装置１、管路a1、酸素
圧縮機２、管路a2、ガスホルダー３の系統は、分
離装置の酸素製造量と使用先Ｕの使用量とがほゞ
等しい場合（使用量の変動がガスホルダー３で吸
収できる場合）である。 In the drawing, the system of air separation device 1, pipe a 1 , oxygen compressor 2, pipe a 2 , and gas holder 3 is shown in Fig. This is the case when fluctuations in usage can be absorbed by the gas holder 3).
酸素使用量が製造量を下回つた場合、即ち、消
費量の変動がガスホルダー３で吸収し得ない場合
には、製出された余剰の酸素ガスは管路b1を経て
液化器４に送られ、液化窒素ガス貯槽から取出さ
れた冷媒窒素と間接熱交換して液化され、管路b2
を経て液化酸素貯槽５に貯えられる。 When the amount of oxygen used falls below the production amount, that is, when the fluctuation in consumption cannot be absorbed by the gas holder 3, the produced surplus oxygen gas is sent to the liquefier 4 via pipe b1. It is sent to the liquefied nitrogen gas storage tank and is liquefied by indirect heat exchange with the refrigerant nitrogen taken out from the liquefied nitrogen gas storage tank .
The liquefied oxygen is then stored in the liquefied oxygen storage tank 5.
また、酸素使用量が製造量を上回つた場合には
液化酸素ガス貯槽５から液化酸素を取出し、管路
b3に設けた液酸ポンプ７により使用圧力まで昇圧
し、酸素熱交換器８で完全に気化され、管路b4を
経て前記管路a2の酸素ガスに合流させる。酸素熱
交換器８において、液化酸素の寒冷は、リサイク
ル圧縮機９で昇圧された窒素ガスに与えられてこ
の窒素ガスを液化する。液化された窒素ガス、即
ち液化窒素は膨張後液化器４に送られ、こゝで冷
媒ガスである分離装置１から管路C1を経て送ら
れた窒素ガスに寒冷を与えて、自らは気化し再び
リサイクル圧縮機９に送られる。前述の如く、液
化器４、管路d2、リサイクル圧縮機９、管路d3、
酸素熱交換器８及び管路d1は閉回路の寒冷サイク
ルを構成している。尚、前記液化器４、酸素熱交
換器８はコールドボツクス１０内に収容する。 In addition, if the amount of oxygen used exceeds the amount produced, liquefied oxygen is taken out from the liquefied oxygen gas storage tank 5 and
The liquid acid is pressurized to the working pressure by the liquid acid pump 7 installed in b 3 , completely vaporized in the oxygen heat exchanger 8, and is made to join the oxygen gas in the pipe a 2 via the pipe b 4 . In the oxygen heat exchanger 8, the refrigeration of the liquefied oxygen is applied to the nitrogen gas pressurized by the recycle compressor 9 to liquefy the nitrogen gas. The liquefied nitrogen gas, that is, the liquefied nitrogen, is sent to the liquefier 4 after expansion, where the nitrogen gas sent from the separation device 1, which is a refrigerant gas, through the pipe C1 is chilled, and the nitrogen gas itself becomes gas. and sent to the recycling compressor 9 again. As mentioned above, the liquefier 4, the pipe d2 , the recycling compressor 9, the pipe d3 ,
The oxygen heat exchanger 8 and the pipe d1 constitute a closed circuit refrigeration cycle. The liquefier 4 and oxygen heat exchanger 8 are housed in a cold box 10.
一方、液化器で液化された窒素は管路c2を経て
冷媒液化窒素貯槽６に貯留され、前記の余剰製品
酸素カスの液化時には、貯槽６から管路c3によつ
て液化器４に送られて寒冷源として使用され、管
路c4から窒素ガス使用先へ送られるか、あるいは
大気中に放出される。 On the other hand, the nitrogen liquefied in the liquefier is stored in the refrigerant liquefied nitrogen storage tank 6 through the pipe c 2 , and when the surplus product oxygen scum is liquefied, it is sent from the storage tank 6 to the liquefier 4 through the pipe c 3 . The nitrogen gas is then used as a cold source and sent through line C4 to the point where the nitrogen gas is used, or it is released into the atmosphere.
本発明による具体的効果を空気分離装置を例と
して以下に説明する。 The specific effects of the present invention will be explained below using an air separation device as an example.
本発明方法によらない、即ち従来のシステムで
は：
(1) 空気分離装置は平均使用量であるO2：
24000Nm3／Ｈで運転されている。 In the conventional system, not according to the method of the present invention: (1) The air separation device uses an average amount of O 2 :
It is operated at 24000Nm 3 /H.
(2) 使用量が、この量を超える時は、増量運転と
なり、最大30000Nm3／Ｈ迄送ガス可能となる。
但し、24000Nm3／Ｈを超える分に対しては、
液酸を蒸発させて供給している。(2) When the amount used exceeds this amount, the amount will be increased and gas can be fed up to a maximum of 30,000Nm 3 /H.
However, for amounts exceeding 24000Nm 3 /H,
Liquid acid is evaporated and supplied.
(3) 使用量が、この量以下の時は、O2圧縮機を
減量し、空気分離装置よりのO2ガスは、
24000Nm3／Ｈにて運転し、余る分は、放風す
るか、又は分離装置全体を減量運転する。(3) When the amount used is less than this amount, the O 2 compressor is reduced and the O 2 gas from the air separation device is
It is operated at 24000Nm 3 /H, and the remaining amount is blown out or the entire separator is operated at reduced capacity.
本発明のシステムを採用することにより：
(1) 本体の空気分離装置は、一定運転
（O224000Nm3／Ｈ）で連続運転され、増減量
の操作が不要となる。 By adopting the system of the present invention: (1) The main air separation device is continuously operated at a constant operation (O 2 24000Nm 3 /H), and there is no need to increase or decrease the amount.
(2) 使用先が増量運転する際の液化酸素の寒冷を
ほとんど回収出来る。例えばO230000Nm3／Ｈ
の増量運転時本来30000−24000＝6000Nm3／Ｈ
の液酸を蒸発させていたため回収出来なかつた
液体のもつているエネルギー（約6000KW・
Ｈ／Ｈに相当）をリサイクル圧縮機等の電力消
費を差引いて4000〜4500KW・Ｈ／Ｈ回収出来
る。これは液化ガス（実装置では液化窒素）と
して、貯槽にためられる。(2) Most of the liquefied oxygen that is cooled when the user increases the amount of liquefied oxygen can be recovered. For example, O 2 30000Nm 3 /H
Normally 30000-24000=6000Nm 3 /H
The energy of the liquid that could not be recovered due to evaporation of the liquid acid (approximately 6000KW)
4000 to 4500 KW/H/H can be recovered by subtracting the electricity consumption of recycling compressors, etc. (equivalent to H/H). This is stored in a storage tank as liquefied gas (liquefied nitrogen in the actual device).
(3) 使用先が、減量運転する際、放風させていた
為のロスがなくなる。例えばO218000Nm3／Ｈ
の減量運転時、本来放風していたO26000N
m3／Ｈを液化器に送り、増量時貯められていた
液化ガス（実装置では、液化窒素）により液化
し、液化酸素として貯槽にため、増量時の使用
に備える。このため空気分離装置の放風ロスが
零とすることができるという非常に大きな長所
がある。(3) When the user performs a reduced-volume operation, the loss caused by blowing air is eliminated. For example, O 2 18000Nm 3 /H
O 2 6000N that was originally released during the reduction operation
m 3 /H is sent to the liquefier, liquefied with the liquefied gas (liquefied nitrogen in the actual device) that was stored during the increase in volume, and stored in a storage tank as liquefied oxygen, ready for use during the increase in volume. Therefore, there is a very great advantage that the air discharge loss of the air separation device can be reduced to zero.
(4) 液化酸素の気化、冷媒窒素ガスの液化はリサ
イクルガスとの熱交換により、酸素ガスの液化
は冷媒液化窒素との熱効換により行われ、空気
分離装置の熱収支バランスとは無関係である。
すなわち、液化ガスや低温ガスを空気分離装置
から取り出したり戻したりすることなく前記の
気化、液化が行えるので、液化、気化工程が空
気分離装置の運転条件に支配されることなく、
使用先における製品ガス使用量の急激な変動に
即座に対応することができる。(4) Vaporization of liquefied oxygen and liquefaction of refrigerant nitrogen gas are performed by heat exchange with recycled gas, and liquefaction of oxygen gas is performed by heat exchange with refrigerant liquefied nitrogen, which is unrelated to the heat balance of the air separation equipment. be.
That is, since the vaporization and liquefaction described above can be performed without taking out or returning the liquefied gas or low-temperature gas from the air separation device, the liquefaction and vaporization processes are not controlled by the operating conditions of the air separation device.
It is possible to immediately respond to sudden changes in the amount of product gas used at the destination.
(5) 前記のように空気分離装置とは全く無関係に
実施できるので、酸素ガスをパイプラインで供
給を受けている需要家の工場内でも本発明の方
法の実施が可能である。この場合、冷媒である
液化窒素は外部から輸送してきて貯槽に供給す
ればよいし、空気分離装置と連通している配管
（パイプライン）は断熱を必要としないので、
その実施には何の困難もない。(5) As described above, the method of the present invention can be carried out completely independently of an air separation device, so it is possible to carry out the method of the present invention even in the factory of a customer who receives oxygen gas through a pipeline. In this case, the refrigerant, liquefied nitrogen, can be transported from outside and supplied to the storage tank, and the piping that communicates with the air separation device does not require insulation.
There will be no difficulty in its implementation.
(6) 空気分離装置とは無関係に、リサイクルガス
量を定めれば、それに見合つた量の酸素ガスを
所望の圧力で供給することができる。この場合
の昇圧には液酸ポンプを使用するので、気化後
に圧縮機で昇圧するのに比して動力費が少くて
すむ。(6) Regardless of the air separation device, if the amount of recycled gas is determined, oxygen gas can be supplied at the desired pressure in an amount commensurate with the amount of recycled gas. Since a liquid acid pump is used to increase the pressure in this case, the power cost is lower than when the pressure is increased using a compressor after vaporization.
以上、空気液化分離装置における酸素及び窒素
を製出する場合について詳述したが、他のガス成
分の組み合せの場合も前記例と同様に操業しうる
ことが明らかである。 The case where oxygen and nitrogen are produced in the air liquefaction separation apparatus has been described in detail above, but it is clear that the same operation as in the above example can also be performed in the case of combinations of other gas components.
添付図面は本発明の一実施例を示すフローシー
トであり、図中、１は空気分離装置、２は酸素圧
縮機、３は酸素ガスホルダー、４は液化器、５は
液化酸素貯槽、６は液化ガス（窒素）貯槽、７は
液酸ポンプ、８は酸素熱交換器、９はリサイクル
圧縮機、Ｕは使用先を示す。
The attached drawing is a flow sheet showing one embodiment of the present invention, and in the drawing, 1 is an air separation device, 2 is an oxygen compressor, 3 is an oxygen gas holder, 4 is a liquefier, 5 is a liquefied oxygen storage tank, and 6 is a flow sheet. A liquefied gas (nitrogen) storage tank, 7 a liquid acid pump, 8 an oxygen heat exchanger, 9 a recycle compressor, and U indicate the place of use.
Claims (1)
給する方法において、製品ガスの使用量が減少し
たときは過剰の製品ガスを製品ガス液化器に導入
して冷媒液化ガスとの間接熱交換により液化して
製品液化ガスとして貯留し、製品ガスの使用量が
増加して製造量では不足したときは前記貯留され
た製品液化ガスを取出し、製品ガス熱交換器でリ
サイクルガスとの間接熱交換により気化して製品
ガスと合流させ使用先に送るとともに、前記熱交
換により冷却されたリサイクルガスを膨張後前記
製品ガス液化器に導入して冷媒ガスと間接熱交換
して昇温し、リサイクル圧縮機を経て前記製品ガ
ス熱交換器に戻す閉回路を形成し、前記熱交換に
より冷却液化された冷媒ガスは冷媒液化ガスとし
て貯留し、前記製品ガス液化時の冷媒として使用
することを特徴とする製品ガス使用量の変動に追
随可能なガス液化及び気化方法。1. In a method of supplying product gas produced by a gas production device, when the amount of product gas used decreases, excess product gas is introduced into a product gas liquefier and liquefied by indirect heat exchange with refrigerant liquefied gas. When the amount of product gas used increases and the production volume is insufficient, the stored product liquefied gas is taken out and vaporized by indirect heat exchange with recycled gas in a product gas heat exchanger. At the same time, the recycled gas cooled by the heat exchange is expanded and introduced into the product gas liquefier, where it is heated by indirect heat exchange with the refrigerant gas, and then passed through the recycling compressor. A closed circuit is formed to return the product gas to the product gas heat exchanger, and the refrigerant gas cooled and liquefied by the heat exchange is stored as a liquefied refrigerant gas and used as a refrigerant when the product gas is liquefied. A gas liquefaction and vaporization method that can follow changes in volume.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58128000A JPS6020073A (en) | 1983-07-15 | 1983-07-15 | Gas liquefying and vaporizing method which can follow to variation of usage of product gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58128000A JPS6020073A (en) | 1983-07-15 | 1983-07-15 | Gas liquefying and vaporizing method which can follow to variation of usage of product gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6020073A JPS6020073A (en) | 1985-02-01 |
| JPH0131116B2 true JPH0131116B2 (en) | 1989-06-23 |
Family
ID=14973976
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58128000A Granted JPS6020073A (en) | 1983-07-15 | 1983-07-15 | Gas liquefying and vaporizing method which can follow to variation of usage of product gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6020073A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5244491B2 (en) * | 2008-07-29 | 2013-07-24 | エア・ウォーター株式会社 | Air separation device |
| JP7446569B2 (en) * | 2020-04-02 | 2024-03-11 | 日本エア・リキード合同会社 | Product gas supply amount adjustment device and air separation device equipped with the same |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2223896A1 (en) * | 1972-05-17 | 1973-11-29 | Sanol Arznei Schwarz Gmbh | PROCESS FOR APPLYING FINE PARTICULAR MEDICINAL PRODUCTS |
| JPS4945998A (en) * | 1972-09-11 | 1974-05-02 |
-
1983
- 1983-07-15 JP JP58128000A patent/JPS6020073A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6020073A (en) | 1985-02-01 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| LAPS | Cancellation because of no payment of annual fees |