JPH11201637A - Air separation method and apparatus - Google Patents
Air separation method and apparatusInfo
- Publication number
- JPH11201637A JPH11201637A JP329498A JP329498A JPH11201637A JP H11201637 A JPH11201637 A JP H11201637A JP 329498 A JP329498 A JP 329498A JP 329498 A JP329498 A JP 329498A JP H11201637 A JPH11201637 A JP H11201637A
- Authority
- JP
- Japan
- Prior art keywords
- oxygen gas
- air
- product
- compressor
- pressure
- 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.)
- Pending
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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
-
- 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
-
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/04—Mixing or blending of fluids with the feed 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the 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
- 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
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
- F25J2240/42—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
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)
Abstract
(57)【要約】
【課題】空気から分離して得た酸素ガスや窒素ガスの放
散を削減し、また減圧によるエネルギー損失を低減でき
る空気分離方法及びその装置を提供する。
【解決手段】圧縮した原料空気を深冷分離して得られた
製品酸素ガスを製品酸素ガス圧縮機６の吸入側から還元
管路１８を通じて原料空気圧縮機１の吸入側に還元す
る。このとき、製品酸素ガス圧縮機６の吸入側の製品酸
素ガス圧力の上昇が所定値以上にならないように、還元
酸素ガス調節装置１９で圧力調整しながら還元酸素ガス
量を制御する。
(57) [Object] To provide an air separation method and an air separation method capable of reducing emission of oxygen gas and nitrogen gas obtained by separating from air and reducing energy loss due to reduced pressure. A product oxygen gas obtained by cryogenically separating compressed raw material air is reduced from a suction side of a product oxygen gas compressor (6) to a suction side of a raw material air compressor (1) through a reduction pipe (18). At this time, the amount of reduced oxygen gas is controlled while the pressure is adjusted by the reduced oxygen gas adjusting device 19 so that the rise of the product oxygen gas pressure on the suction side of the product oxygen gas compressor 6 does not exceed a predetermined value.
Description
【０００１】[0001]
【発明の属する技術分野】本発明は原料空気を主として
酸素と窒素とに分離する空気分離方法及びその装置に関
し、特に余剰となった酸素の処理に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an air separation method for separating raw air into oxygen and nitrogen mainly, and an apparatus therefor, and more particularly to the treatment of excess oxygen.
【０００２】[0002]
【従来の技術】この種の空気分離装置としては、例えば
図２に示すようなものがある。この空気分離装置では、
まず原料空気流量計２ａ，原料空気流量調節計２ｂ並び
に原料空気流量調節弁２ｃからなる原料空気流量制御装
置２によって原料空気圧縮機１の吐出側の流量をフィー
ドバック制御しながら、当該原料空気圧縮機１で原料空
気を圧縮して熱交換器３に送給する。この熱交換器３で
は、既に分離された低温の製品（空気を分離して得た酸
素ガスや窒素ガスを、以下、製品酸素ガス或いは製品窒
素ガスなどとも称する）酸素ガスＯ2 や製品窒素ガスＮ
2 によって、圧縮された原料空気が冷却され、その中で
固化分離した水分や炭酸ガスが除去されてから空気液化
分離器４に送給される。この空気液化分離器４で深冷分
離された製品酸素ガスＯ2 は、前記熱交換器３を経由す
る製品酸素ガス送給管路５を介して製品酸素ガス圧縮機
６によって圧縮され、高圧製品酸素ガスＯ2 として高圧
製品酸素ガス送給管路７を介して使用先に送給されると
共に、その一部は製品酸素ガスホルダ８に貯蔵される。
一方、前記空気液化分離器４で分離された製品窒素ガス
Ｎ2 は、やはり前記前記熱交換器３を経由する製品窒素
ガス送給管路１１を介して製品窒素ガス圧縮機１２によ
って圧縮され、高圧製品窒素ガスＮ2 として高圧製品窒
素ガス送給管路１３を介して使用先に送給される。な
お、前記空気液化分離器４内で余剰の液体酸素が発生し
た場合には、液体酸素送給管路９を介して液体酸素貯槽
１０に貯蔵可能である。また、気化した製品酸素ガスＯ
2 は、製品酸素ガス圧縮機６の吸入側及び吐出側の夫々
に設けられた吸入側製品酸素放散弁１４及び吐出側製品
酸素放散弁１５から大気放散される。ちなみに、図中の
符号１６は空気を断熱膨張させ、寒冷を発生させるため
の膨張タービン，符号１７は断熱膨張用空気送給管路で
ある。2. Description of the Related Art An example of this type of air separation apparatus is shown in FIG. In this air separation device,
First, the feed air flow compressor 2 is fed back to the feed air compressor 1 while the flow rate on the discharge side of the feed air compressor 1 is feedback-controlled by the feed air flow controller 2 including the feed air flow meter 2a, the feed air flow controller 2b and the feed air flow control valve 2c. The raw material air is compressed in 1 and sent to the heat exchanger 3. In the heat exchanger 3, already separated cold products (oxygen gas or nitrogen gas obtained by separation of air, hereinafter also referred to as product oxygen gas or nitrogen product gas) oxygen gas O 2 and nitrogen product gas N
By 2 , the compressed raw material air is cooled and water and carbon dioxide solidified and separated therein are removed, and then sent to the air liquefaction separator 4. The product oxygen gas O 2 cryogenically separated by the air liquefaction separator 4 is compressed by a product oxygen gas compressor 6 through a product oxygen gas supply line 5 passing through the heat exchanger 3, and a high pressure product The oxygen gas is supplied as oxygen gas O 2 through a high-pressure product oxygen gas supply line 7 to a use destination, and a part of the oxygen gas is stored in a product oxygen gas holder 8.
On the other hand, the product nitrogen gas N 2 separated by the air liquefaction separator 4 is compressed by the product nitrogen gas compressor 12 via the product nitrogen gas supply pipe 11 which also passes through the heat exchanger 3, The high-pressure product nitrogen gas N 2 is supplied to the place of use through the high-pressure product nitrogen gas supply line 13. When excess liquid oxygen is generated in the air liquefaction separator 4, it can be stored in the liquid oxygen storage tank 10 via the liquid oxygen supply pipe 9. In addition, the vaporized product oxygen gas O
2 is released to the atmosphere from a product oxygen release valve 14 and a product oxygen release valve 15 provided on the suction side and the discharge side of the product oxygen gas compressor 6, respectively. Incidentally, reference numeral 16 in the drawing denotes an expansion turbine for adiabatically expanding air to generate cold, and reference numeral 17 denotes an air supply pipe for adiabatic expansion.
【０００３】[0003]
【発明が解決しようとする課題】ところで、製品酸素ガ
スＯ2 の使用先での消費量，つまり需要が減少するとき
には、前記空気液化分離器４によって分離する製品酸素
ガスＯ2 の量そのものを減少させるが、このとき前述し
た原料空気圧縮機１の機械的な制約から、実質的に約３
０％程度しか分離される製品酸素ガスＯ2 の量を減少で
きない。また、前記製品酸素ガスホルダ８に貯蔵できる
製品酸素ガスＯ2 の量にも自ずと限界がある。従って、
これ以上に余剰な製品酸素ガスＯ2 は、前記吸入側製品
酸素放散弁１４及び吐出側製品酸素放散弁１５から大気
に放散するしかない。By the way, when the consumption of the product oxygen gas O 2 at the place of use, that is, the demand decreases, the amount of the product oxygen gas O 2 separated by the air liquefaction separator 4 itself decreases. However, at this time, due to the mechanical restriction of the raw material air compressor 1 described above, substantially about 3
About 0% only can reduce the amount of product oxygen gas O 2 to be separated. Further, the amount of the product oxygen gas O 2 that can be stored in the product oxygen gas holder 8 is naturally limited. Therefore,
The surplus product oxygen gas O 2 can only be released from the suction side product oxygen release valve 14 and the discharge side product oxygen release valve 15 to the atmosphere.
【０００４】このような問題を解決するために、例えば
特公昭４９−４５９９７号公報や特公昭４９−４５９９
８号公報に記載される空気分離方法や装置がある。この
公報に記載される空気分離方法及び装置では、分離され
た酸素と窒素とを夫々液体状態で貯蔵できる貯槽を有
し、例えば製品酸素ガスＯ2 を増加する場合には、製品
窒素ガスＮ2 との熱交換によって液体酸素を気化し、製
品酸素ガスＯ2 を減少する場合には、液体窒素による冷
熱の回収により製品酸素ガスＯ2 を液化して貯蔵するよ
うにしている。しかしながら、この従来技術によれば、
特に製品酸素ガスＯ2 を減少させるとき、当該製品酸素
ガスＯ2 の液化に伴って発生する気化した窒素ガスＮ2
が利用されることなく放散されるという問題がある。To solve such a problem, for example, Japanese Patent Publication No. 49-45997 and Japanese Patent Publication No. 49-4599
No. 8 discloses an air separation method and apparatus. The air separation method and apparatus described in this publication have storage tanks capable of storing separated oxygen and nitrogen in a liquid state, respectively. For example, when increasing the product oxygen gas O 2 , the product nitrogen gas N 2 the liquid oxygen is vaporized by heat exchange with, in the case of reducing the oxygen product gas O 2 is designed so as to store liquefied product oxygen gas O 2 by the recovery of cold liquid nitrogen. However, according to this prior art,
In particular product when reducing oxygen gas O 2, the product oxygen gas O nitrogen gas N 2, which with the liquefied vaporized to generate the 2
There is a problem that is dissipated without being used.
【０００５】また、この他にも本出願人が先に提案した
特開平５−３４０６１号公報に記載される空気分離方法
及び装置では、図２に二点鎖線で示すように、前記製品
酸素ガス圧縮機６の吐出側から前記原料空気圧縮機１の
吐出側に余剰な製品酸素ガスＯ2 を還元する（単に入側
に戻すといった意味であり、製品酸素ガスを原料空気側
に戻すことを還元と記し、その酸素ガスを還元酸素ガス
とも記す）。しかしながら、例えば製鉄所においては、
吹錬に対応するために、前記製品酸素ガス圧縮機６の吐
出圧は２５kg/cm2程度であり、片や前記原料空気圧縮機
１の吐出圧は５kg/cm2程度であることから、当該製品酸
素ガス圧縮機６の吐出側から前記原料空気圧縮機１の吐
出側に製品酸素ガスＯ2 を還元する場合には、わざわざ
高圧化した製品酸素ガスＯ2 を再び減圧するというエネ
ルギー損失がある。[0005] In addition, in the air separation method and apparatus described in Japanese Patent Application Laid-Open No. Hei 5-34061, which was previously proposed by the present applicant, as shown by a two-dot chain line in FIG. The excess product oxygen gas O 2 is reduced from the discharge side of the compressor 6 to the discharge side of the raw material air compressor 1 (this means simply returning to the inlet side, and returning the product oxygen gas to the raw material air side is reduced). And the oxygen gas is also referred to as reduced oxygen gas). However, for example, in steelworks,
In order to cope with blowing, the discharge pressure of the product oxygen gas compressor 6 is about 25 kg / cm 2 , and the discharge pressure of the piece or the raw material air compressor 1 is about 5 kg / cm 2. When reducing the product oxygen gas O 2 from the discharge side of the product oxygen gas compressor 6 to the discharge side of the raw material air compressor 1, there is an energy loss that the pressure of the product oxygen gas O 2, which has been increased in pressure, is reduced again. .
【０００６】本発明はこれらの諸問題に鑑みて開発され
たものであり、わざわざ分離した酸素ガスや窒素ガスを
放散することを抑制し、また高圧化した酸素ガスＯ2 を
減圧するといったエネルギー損失を小さくすることがで
きる空気分離方法及びその装置を提供することを目的と
するものである。[0006] The present invention has been developed in view of these problems, and suppresses the emission of separately separated oxygen gas and nitrogen gas, and reduces the energy loss such as reducing the pressure of oxygen gas O 2 at high pressure. It is an object of the present invention to provide an air separation method and an apparatus thereof that can reduce the size.
【０００７】[0007]
【課題を解決するための手段】上記問題を解決するため
に、本発明のうち請求項１に係る空気分離方法は、空気
を分離して得た酸素ガスのうち、余剰となった酸素ガス
を、原料空気を圧縮する原料空気圧縮機の吸入側に還元
することを特徴とするものである。In order to solve the above-mentioned problems, an air separation method according to a first aspect of the present invention is a method for separating excess oxygen gas from oxygen gas obtained by separating air. The feed air is reduced to the suction side of a feed air compressor that compresses the feed air.
【０００８】また、本発明のうち請求項２に係る空気分
離装置は、空気を分離して得た酸素ガスを圧縮する酸素
ガス圧縮機の吸入側と原料空気を圧縮する原料空気圧縮
機の吸入側とを連結する還元管路と、前記酸素ガス圧縮
機の吸入側における酸素ガスの圧力の上昇を所定値以下
に保持するように、前記還元管路に設けられた調節弁を
調節して、余剰となった酸素ガスを、前記原料空気圧縮
機の吸入側に還元する調節装置を備えたことを特徴とす
るものである。In the air separation apparatus according to a second aspect of the present invention, the suction side of an oxygen gas compressor for compressing oxygen gas obtained by separating air and the suction of a raw air compressor for compressing raw material air are provided. A control valve provided in the reduction line so as to maintain a rise in pressure of oxygen gas at a suction side of the oxygen gas compressor at a predetermined value or less, An adjusting device is provided for reducing excess oxygen gas to the suction side of the raw material air compressor.
【０００９】[0009]
【発明の実施の形態】次に、本発明に係る空気分離方法
及びその装置の一実施形態について図面を用いながら説
明する。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Next, an embodiment of an air separation method and apparatus according to the present invention will be described with reference to the drawings.
【００１０】図１には本実施形態の空気分離装置の概要
を示す。この空気分離装置の概略構成は、前記図２に示
す従来のものと同様であるので、同等の構成には同等の
符号を附して、その詳細な説明を省略する。FIG. 1 shows an outline of an air separation apparatus according to this embodiment. Since the schematic configuration of this air separation device is the same as that of the conventional one shown in FIG. 2, the same components are denoted by the same reference numerals and detailed description thereof will be omitted.
【００１１】この実施形態では、まず前記製品酸素ガス
圧縮機６の吸入側と原料空気圧縮機１の吸入側，より厳
密には前記原料空気流量制御装置２の原料空気流量調節
弁２ｃより更に入側とを、酸素ガス還元管路１８で連結
すると共に、この還元管路１８には還元酸素ガス流量調
節装置１９のアクチュエータとして圧力調節弁１９ｃを
介装する。また、この還元管路１８の入側には、還元酸
素ガス流量調節装置１９の検出器としての製品酸素ガス
圧力計１９ａを取付け、製品酸素ガス圧縮機６の吸入
側，つまり熱交換器３で得られる製品酸素ガスＯ2 の圧
力を検出する。そして、還元酸素ガス流量調節装置１９
のコントローラである還元酸素ガス流量調節計１９ｂ
は、前記還元酸素ガス圧力計１９ａで検出される製品酸
素ガスＯ2 の圧力の上昇が所定値以下になるように、即
ち製品酸素ガスＯ2 の圧力が所定値を越えないように、
前記圧力調節弁１９ｃの開度を調節して当該製品酸素ガ
スＯ2の圧力を制御する。In this embodiment, first, the suction side of the product oxygen gas compressor 6 and the suction side of the raw material air compressor 1, more precisely, the raw material air flow rate control valve 2 c of the raw material air flow control device 2 are further input. The side is connected with an oxygen gas reducing pipe 18, and a pressure control valve 19 c is interposed in the reducing pipe 18 as an actuator of a reducing oxygen gas flow rate adjusting device 19. A product oxygen gas pressure gauge 19a as a detector of the reduced oxygen gas flow rate control device 19 is attached to the inlet side of the reduction pipe line 18, and is connected to the suction side of the product oxygen gas compressor 6, that is, the heat exchanger 3. The pressure of the obtained product oxygen gas O 2 is detected. Then, the reducing oxygen gas flow rate adjusting device 19
Oxygen gas flow controller 19b which is the controller of
Is set so that the increase in the pressure of the product oxygen gas O 2 detected by the reducing oxygen gas pressure gauge 19a is equal to or less than a predetermined value, that is, so that the pressure of the product oxygen gas O 2 does not exceed a predetermined value.
Controlling the pressure of the product oxygen gas O 2 by adjusting an opening degree of the pressure regulating valve 19c.
【００１２】これにより、余剰の製品酸素ガスＯ2 だけ
が、一旦原料空気側に還元され、それらが前記原料空気
圧縮機１で圧縮される。一方、空気液化分離器４に送ら
れた余剰酸素は内部で液化され、前記液体酸素送給管路
９を介して液体酸素貯槽１０に貯蔵される。従って、熱
交換器３の出側における余剰な製品酸素ガスＯ2 ，即ち
製品酸素ガス圧縮機６の吸入側の余剰な製品酸素ガスＯ
2 は、高圧に圧縮される以前に原料空気に還元，混入さ
れるので、その減圧代は、前記製品酸素ガス圧縮機６の
吐出側の高圧製品酸素ガスＯ2 を原料空気圧縮機１の吐
出側に還元するよりも小さい。As a result, only the excess product oxygen gas O 2 is once reduced to the raw material air side, and these are compressed by the raw material air compressor 1. On the other hand, surplus oxygen sent to the air liquefaction separator 4 is liquefied inside and stored in the liquid oxygen storage tank 10 via the liquid oxygen supply pipe 9. Therefore, surplus product oxygen gas O 2 on the outlet side of the heat exchanger 3, that is, surplus product oxygen gas O 2 on the suction side of the product oxygen gas compressor 6.
2 is reduced and mixed into the raw material air before it is compressed to a high pressure, so that the decompression allowance is that the high pressure product oxygen gas O 2 on the discharge side of the product oxygen gas compressor 6 is discharged from the raw material air compressor 1. Smaller than reducing to the side.
【００１３】より具体的には、例えば前述のように原料
空気圧縮機１の吐出圧が５kg/cm2程度、熱交換器３の出
側，即ち製品酸素ガス圧縮機６の吸入圧が０．２kg/cm2
程度、製品酸素ガス圧縮機６の吐出圧が２５kg/cm2程度
で、例えば原料空気圧縮機１の処理量が１０００００〜
１４３０００Ｎm3/h，製品酸素ガスの発生量が２０００
０〜２８６００Ｎm3/h，製品酸素ガス圧縮機（複数機に
より構成）の処理量が０〜３００００Ｎm3/hという条件
下で、２０００Ｎm3/hの余剰な製品酸素ガスＯ 2 が発生
した場合の本実施形態の減圧損失は１００kW程度の減圧
損失になる。一方、前記製品酸素ガス圧縮機６の吐出側
の高圧製品酸素ガスＯ2 を原料空気圧縮機１の吐出側に
還元する従来技術で１７１kW程度の減圧損失が生じるか
ら、その差は７１kW程度で約４２％の損失低減が可能と
なる。More specifically, for example, as described above,
The discharge pressure of the air compressor 1 is 5kg / cmTwoDegree, exit of heat exchanger 3
Side, that is, the suction pressure of the product oxygen gas compressor 6 is 0.2 kg / cmTwo
Degree, discharge pressure of product oxygen gas compressor 6 is 25kg / cmTwodegree
Thus, for example, the throughput of the raw material air compressor 1 is 100,000 to
143000NmThree/ h, product oxygen gas generation is 2000
0 to 28600 NmThree/ h, product oxygen gas compressor (for multiple machines)
From 3 to 30 NmThree/ h condition
Below, 2000NmThree/ h surplus product oxygen gas O TwoOccurs
In this case, the decompression loss of this embodiment is about 100 kW
Results in losses. On the other hand, the discharge side of the product oxygen gas compressor 6
High pressure product oxygen gas OTwoTo the discharge side of the raw material air compressor 1.
Is the decompression loss of about 171 kW caused by the conventional technology of reduction?
The difference is about 71kW and about 42% loss reduction is possible.
Become.
【００１４】勿論、余剰な製品酸素ガスＯ2 も製品窒素
ガスＮ2 も無駄に放散する必要はない。Needless to say, it is not necessary to uselessly emit the excess product oxygen gas O 2 and the product nitrogen gas N 2 .
【００１５】[0015]
【発明の効果】以上説明したように、本発明のうち請求
項１に係る空気分離方法によれば、余剰となった酸素ガ
スを、原料空気を圧縮する原料空気圧縮機の吸入側に還
元するようにしたため、過酸素状態で圧縮された原料空
気は、その酸素成分だけが、例えば空気液化分離器にお
いて液体酸素として回収されるので、前記余剰となった
酸素ガスや窒素ガスの放散を抑制でき、わざわざ高圧化
した酸素ガスを減圧するといったエネルギー損失を小さ
くすることができる。As described above, according to the air separation method of the first aspect of the present invention, surplus oxygen gas is reduced to the suction side of the raw air compressor for compressing the raw air. Because of this, the raw air compressed in the peroxygen state, only the oxygen component is recovered as liquid oxygen in, for example, an air liquefaction separator, so that the emission of the surplus oxygen gas and nitrogen gas can be suppressed. In addition, it is possible to reduce energy loss such as depressurizing the oxygen gas which has been purposely increased in pressure.
【００１６】また、本発明のうち請求項２に係る空気分
離装置によれば、酸素ガス圧縮機の吸入側における酸素
ガスの圧力の上昇を所定値以下に保持するように、前記
還元管路に設けられた調節弁を調節して、余剰となった
酸素ガスだけを原料空気圧縮機の吸入側に還元するよう
にしたため、過酸素状態で圧縮された原料空気は、その
酸素成分だけが、例えば空気液化分離器において液体酸
素として回収されるので、前記余剰となった酸素ガスや
窒素ガスの放散を削減でき、わざわざ高圧化した酸素ガ
スを減圧するといったエネルギー損失を小さくすること
ができる。Further, according to the air separation device of the second aspect of the present invention, the pressure in the reduction conduit is controlled so as to keep the increase in the pressure of the oxygen gas on the suction side of the oxygen gas compressor at a predetermined value or less. Since the control valve provided was adjusted so that only the excess oxygen gas was reduced to the suction side of the raw air compressor, the raw air compressed in the peroxygen state had only its oxygen component, for example. Since it is recovered as liquid oxygen in the air liquefaction separator, it is possible to reduce the emission of the excess oxygen gas and nitrogen gas, and to reduce energy loss such as depressurizing the oxygen gas which has been purposely increased in pressure.
【図１】本発明の空気分離方法及びその装置の一実施形
態を示す概略構成図である。FIG. 1 is a schematic configuration diagram showing an embodiment of an air separation method and an apparatus thereof according to the present invention.
【図２】従来の空気分離方法及びその装置の概略説明図
である。FIG. 2 is a schematic explanatory view of a conventional air separation method and its apparatus.
１は原料空気圧縮機 ２は原料空気流量制御装置 ３は熱交換器 ４は空気液化分離器 ５は製品酸素ガス送給管路 ６は製品酸素ガス圧縮機 ７は高圧製品酸素ガス送給管路 ８は製品酸素ガスホルダ ９は液体酸素送給管路 １０は液体酸素貯槽 １１は製品窒素ガス送給管路 １２は製品窒素ガス圧縮機 １３は高圧製品窒素ガス送給管路 １４は吸入側製品酸素放散弁 １５は吐出側製品酸素放散弁 １６は膨張タービン １７は断熱膨張用空気送給管路 １８は酸素ガス還元管路 １９は還元酸素ガス流量調節装置 1 is a raw air compressor 2 is a raw air flow control device 3 is a heat exchanger 4 is an air liquefaction separator 5 is a product oxygen gas supply line 6 is a product oxygen gas compressor 7 is a high pressure product oxygen gas supply line 8 is a product oxygen gas holder 9 is a liquid oxygen supply line 10 is a liquid oxygen storage tank 11 is a product nitrogen gas supply line 12 is a product nitrogen gas compressor 13 is a high pressure product nitrogen gas supply line 14 is a suction side product oxygen The release valve 15 is a discharge side product oxygen release valve 16 is an expansion turbine 17 is an adiabatic expansion air supply pipeline 18 is an oxygen gas reduction pipeline 19 is a reduced oxygen gas flow control device
Claims (2)
剰となった酸素ガスを、原料空気を圧縮する原料空気圧
縮機の吸入側に還元することを特徴とする空気分離方
法。1. An air separation method comprising reducing excess oxygen gas among oxygen gas obtained by separating air to a suction side of a raw material air compressor for compressing raw material air.
酸素ガス圧縮機の吸入側と原料空気を圧縮する原料空気
圧縮機の吸入側とを連結する還元管路と、前記酸素ガス
圧縮機の吸入側における酸素ガスの圧力の上昇を所定値
以下に保持するように、前記還元管路に設けられた調節
弁を調節して、余剰となった酸素ガスを、前記原料空気
圧縮機の吸入側に還元する調節装置を備えたことを特徴
とする空気分離装置。2. A reduction line connecting an intake side of an oxygen gas compressor for compressing oxygen gas obtained by separating air and an intake side of a raw air compressor for compressing raw air; The control valve provided in the reduction conduit is adjusted so that the increase in the pressure of the oxygen gas on the suction side of the machine is maintained at a predetermined value or less, and the excess oxygen gas is removed from the feed air compressor. An air separation device comprising an adjustment device for reducing on the suction side.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP329498A JPH11201637A (en) | 1998-01-09 | 1998-01-09 | Air separation method and apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP329498A JPH11201637A (en) | 1998-01-09 | 1998-01-09 | Air separation method and apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH11201637A true JPH11201637A (en) | 1999-07-30 |
Family
ID=11553373
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP329498A Pending JPH11201637A (en) | 1998-01-09 | 1998-01-09 | Air separation method and apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH11201637A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2011046557A (en) * | 2009-08-26 | 2011-03-10 | Jfe Steel Corp | Apparatus and method for supplying oxygen |
-
1998
- 1998-01-09 JP JP329498A patent/JPH11201637A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2011046557A (en) * | 2009-08-26 | 2011-03-10 | Jfe Steel Corp | Apparatus and method for supplying oxygen |
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