JPS647001B2 - - Google Patents
Info
- Publication number
- JPS647001B2 JPS647001B2 JP55027956A JP2795680A JPS647001B2 JP S647001 B2 JPS647001 B2 JP S647001B2 JP 55027956 A JP55027956 A JP 55027956A JP 2795680 A JP2795680 A JP 2795680A JP S647001 B2 JPS647001 B2 JP S647001B2
- Authority
- JP
- Japan
- Prior art keywords
- oxygen
- flow rate
- pressure
- adsorption
- mixed gas
- 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
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 149
- 239000001301 oxygen Substances 0.000 claims abstract description 149
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 149
- 239000007789 gas Substances 0.000 claims abstract description 27
- 238000001179 sorption measurement Methods 0.000 claims description 47
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 22
- 238000000034 method Methods 0.000 claims description 19
- 229910052757 nitrogen Inorganic materials 0.000 claims description 11
- 230000036284 oxygen consumption Effects 0.000 claims description 9
- 239000003463 adsorbent Substances 0.000 claims description 2
- 238000003795 desorption Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 3
- 230000002745 absorbent Effects 0.000 abstract 1
- 239000002250 absorbent Substances 0.000 abstract 1
- 239000002994 raw material Substances 0.000 description 7
- 230000007423 decrease Effects 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- 238000001514 detection method Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000004044 response Effects 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 description 1
- LGRFSURHDFAFJT-UHFFFAOYSA-N Phthalic anhydride Natural products C1=CC=C2C(=O)OC(=O)C2=C1 LGRFSURHDFAFJT-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 238000004378 air conditioning Methods 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- JHIWVOJDXOSYLW-UHFFFAOYSA-N butyl 2,2-difluorocyclopropane-1-carboxylate Chemical compound CCCCOC(=O)C1CC1(F)F JHIWVOJDXOSYLW-UHFFFAOYSA-N 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000012258 culturing Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M23/00—Constructional details, e.g. recesses, hinges
- C12M23/36—Means for collection or storage of gas; Gas holders
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/06—Nozzles; Sprayers; Spargers; Diffusers
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
- C12M29/26—Conditioning fluids entering or exiting the reaction vessel
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
- C12M41/30—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration
- C12M41/34—Means for regulation, monitoring, measurement or control, e.g. flow regulation of concentration of gas
Landscapes
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Organic Chemistry (AREA)
- Wood Science & Technology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Zoology (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Sustainable Development (AREA)
- Microbiology (AREA)
- Biotechnology (AREA)
- Biochemistry (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Biomedical Technology (AREA)
- Clinical Laboratory Science (AREA)
- Analytical Chemistry (AREA)
- Oxygen, Ozone, And Oxides In General (AREA)
- Apparatus Associated With Microorganisms And Enzymes (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
Description
本発明は、酸素濃縮装置を備えた酸素の利用装
置における酸素流量の制御方法ならびに制御装置
に関する。
濃縮ないしは精製された酸素は酢酸、エチレン
オキサイドおよび無水フタル酸の製造等のような
化学工業、各種の炉への吹き込み、醗酵工業、廃
水処理、空調、医療分野等の用途において広く用
いられており、かかる用途における酸素純度はい
ずれも95％以下で充分である。
このような用途の酸素利用装置に対して濃縮酸
素を供給するために、原料しての空気中に含まれ
るチツ素を選択的に吸着および脱着する差圧吸着
法が一般的に用いられている。従来、この操作は
固定された一定の圧力下で行なわれているため
に、利用装置の酸素消費量の如何に拘わらず常に
同一流量の酸素が供給されることになり、酸素負
荷低下の場合には加圧空気が無駄に使用されて著
しい損失を生じていた。
かかる利用装置の酸素負荷変動に対応する手段
として、たとえば吸着系の除湿装置の切替時間を
負荷の低い夜間のみ長くして加圧空気の損失を減
少させる方法が知られている（特開昭50−161466
号）。しかし、この方法でも切替は２段階にしか
設定されないので急激な負荷変動には充分に対応
できない欠点があつた。
本発明の目的は、このような従来技術の欠点を
解消し、酸素を利用する装置の負荷の変動に対応
して常に酸素を適正な流量で供給することのでき
る酸素の利用装置における供給酸素流量の制御方
法ならびに制御装置を提供することにある。
本発明は、酸素の利用装置における酸素負荷の
変動に対して原料ガスの送入圧力を調整すること
により、消費量に適合した流量の酸素を一定の酸
素濃度下で供給することが可能であるという本発
明者等の研究および実験によつて得られた知見に
基づいてなされたものである。
すなわち本発明の特色は、チツ素および酸素を
主要な成分として含む混合ガスを少なくともその
中の一つの成分に対して選択的な吸着性を有する
吸着物質を含む吸着塔内に加圧送入し、差圧吸着
法により分離して濃縮された酸素を含むガスを生
成し、これを酸素の利用装置に一定の所要酸素濃
度下で供給する方法において、前記利用装置に供
給される酸素流量および前記利用装置から放出さ
れる酸素濃度を夫々検出し、前記酸素濃度の検出
値および前記酸素流量の検出値に基づいて利用装
置における酸素消費量を算出し、該酸素消費量に
基づいて所要酸素濃度下で前記利用装置へ供給し
なければならない供給酸素流量を算出し、該供給
酸素流量と前記所要酸素濃度とに基づいて前記吸
着塔へ送入する混合ガスの送入圧力を求め、求め
られた該送入圧力に基づいて吸着塔へ送入する前
記混合ガスの送入圧力を調整し、それによつて前
記供給酸素流量を制御することにある。
さらに本発明の別の特色は、チツ素および酸素
を主要な成分として含む混合ガスを加圧送入する
圧送ポンプ、前記混合ガス中の少なくとも一つの
成分に対して選択的な吸着性を有する吸着物質で
充填された吸着塔、および前記吸着塔中で吸着工
程および脱着工程を反復させて差圧吸着法により
濃縮された酸素を含むガスを生成して供給するた
めの切換制御系からなる酸素濃縮装置を備えた酸
素の利用装置において、前記酸素濃縮装置から前
記利用装置に供給される酸素流量を検出する流量
計と、前記利用装置から放出される酸素濃度を検
出する濃度検知器と、前記流量計で検出された酸
素流量および前記濃度検知器で検出された酸素濃
度から算出される酸素消費量の夫々の値を演算処
理し、この演算結果に基づいて酸素消費量に対応
する酸素流量が供給されるように前記圧送ポンプ
の加圧動作を調整する制御装置を設けたことにあ
る。
以下本発明の一実施例を図面に基づいて詳細に
説明する。
第１図は、酸素濃縮装置を備えた培養槽に本発
明を適用した実施例の系統図を示す。図中、酸素
濃縮装置の主体をなすチツ素吸着塔１，２の入口
側には送入管３から送られた空気を加圧して供給
する送圧ポンプ４が水滴分離器５および弁６，８
を介して結合されている。また前記チツ素吸着塔
１，２の出口側は夫々弁１０，１１を介して酸素
タンク１２に結合されており、ここから取出し管
１３を経て酸素の利用装置としての培養槽１６に
導かれている。その他図中、７，９は各吸着塔
１，２の排気弁を示す。
培養槽１６には前記吸着塔１，２から供給され
る濃縮酸素が導入される供給口１５および槽から
の排気を放出する排気口１７が設けられており、
供給される酸素は培養液１８の液中の下方に設置
されたスパージヤ２０から散気され、インペラ２
１で撹拌されながら液中を上昇して排気される。
図中、２２はバツフル板、２３はインペラの回転
駆動機構である。
ここで本実施例においては、前記チツ素吸着塔
１，２からの取出し管１３と培養槽１６の供給口
１５との間に供給される酸素流量を検知する電磁
流量計１４が設けられており、また培養槽１６の
排気口１７中には放出される排気中の酸素濃度を
検出するセンサ１９が設置されている。これら電
磁流量計１４および酸素濃度のセンサ１９からの
検知電気信号は制御装置２４に対して夫々電気的
に結合されている。制御装置２４はセンサ１９か
らの酸素濃度の検知信号に基づいて培養槽１６中
での消費酸素量を算出し、算出された消費酸素
量、すなわち培養槽１６中の所要酸素量について
のデータと前記流量計１４で検知された各時点で
の実際の供給酸素量のデータとに基づく制御信号
を発生する回路を備えている。前記制御信号は送
圧ポンプ４の回転数可変制御部に電気的に接続さ
れている。
以下、このような本発明の実施例装置の動作に
ついて説明する。
まず吸着塔１が加圧吸着工程にまた吸着塔２が
減圧工程になされる。このため弁６，９，１０が
開放され、また弁７，８，１１が閉じられる。こ
れらの弁の切換操作で送入管３からの空気が送圧
ポンプ４で加圧され水滴分離器５で除湿された
後、弁６を介して吸着塔１に送られる。吸着塔１
では加圧空気中のチツ素が選択的に吸着され、酸
素は弁１０を通つて酸素タンク１２に送られる。
一方、この間に減圧工程にある吸着塔２は弁９に
よつて大気側に開放され、前段のサイクルでこの
吸着塔２中に吸着されていたチツ素が系外に排気
される（操作サイクルNo.１）。
次いで吸着塔１が減圧排気工程に、吸着塔２が
均圧化工程に夫々切換えられる。この場合には弁
７，１１が開放され弁６，８，９，１０が閉じら
れる。これらの弁切換え操作で吸着塔１は弁７に
よつて大気側に開放され、この吸着塔中に吸着さ
れたチツ素が系外に排気される。一方、酸素タン
ク１２に貯蔵されている酸素の一部が弁１１を通
つて吸着塔２に返送される（操作サイクルNo.２）。
以下同様にして各工程が吸着塔１，２について
操作サイクルNo.３、No.４として反復される。この
状態を下表に示す。
The present invention relates to a method and a control device for controlling an oxygen flow rate in an oxygen utilization device including an oxygen concentrator. Concentrated or purified oxygen is widely used in the chemical industry, such as in the production of acetic acid, ethylene oxide, and phthalic anhydride, as well as in the blowing into various furnaces, the fermentation industry, wastewater treatment, air conditioning, and the medical field. In all such applications, oxygen purity of 95% or less is sufficient. In order to supply concentrated oxygen to oxygen utilization equipment for such applications, a differential pressure adsorption method that selectively adsorbs and desorbs nitrogen contained in the air as a raw material is generally used. . Conventionally, this operation is carried out under a fixed, constant pressure, which means that the same flow rate of oxygen is always supplied regardless of the oxygen consumption of the equipment used, and in the event of a decrease in oxygen load. Pressurized air was wasted, resulting in significant losses. As a means of dealing with oxygen load fluctuations in such utilization equipment, a method is known in which, for example, the switching time of an adsorption-type dehumidifier is lengthened only at night when the load is low to reduce the loss of pressurized air (Japanese Patent Application Laid-Open No. 1983-1993). −161466
issue). However, even with this method, the switching is only set in two stages, so there is a drawback that it cannot adequately cope with rapid load fluctuations. An object of the present invention is to solve the drawbacks of the prior art and to improve the flow rate of oxygen in an oxygen utilization device, which can always supply oxygen at an appropriate flow rate in response to changes in the load of the oxygen utilization device. An object of the present invention is to provide a control method and a control device. The present invention makes it possible to supply oxygen at a flow rate that matches the consumption amount under a constant oxygen concentration by adjusting the feeding pressure of the raw material gas in response to changes in the oxygen load in the oxygen utilization device. This was made based on the findings obtained through research and experiments by the present inventors. That is, the feature of the present invention is that a mixed gas containing nitrogen and oxygen as main components is fed under pressure into an adsorption tower containing an adsorption material that has selective adsorption properties for at least one of the components, A method in which a gas containing concentrated oxygen is separated and concentrated by a differential pressure adsorption method and is supplied to an oxygen utilization device at a constant required oxygen concentration, the oxygen flow rate supplied to the utilization device and the utilization Detecting the oxygen concentration released from each device, calculating the oxygen consumption amount in the utilization device based on the detected oxygen concentration value and the detected oxygen flow rate value, and calculating the oxygen consumption amount under the required oxygen concentration based on the oxygen consumption amount. Calculate the supply oxygen flow rate that must be supplied to the utilization equipment, determine the supply pressure of the mixed gas to be supplied to the adsorption tower based on the supply oxygen flow rate and the required oxygen concentration, and The purpose of the present invention is to adjust the feeding pressure of the mixed gas fed to the adsorption tower based on the input pressure, and thereby control the supplied oxygen flow rate. Furthermore, another feature of the present invention is a pressure pump that feeds a mixed gas containing nitrogen and oxygen as main components under pressure; An oxygen concentrator consisting of an adsorption tower filled with gas, and a switching control system for repeating the adsorption step and desorption step in the adsorption tower to generate and supply a gas containing concentrated oxygen by differential pressure adsorption method. An oxygen utilization device comprising: a flowmeter that detects the flow rate of oxygen supplied from the oxygen concentrator to the utilization device; a concentration detector that detects the concentration of oxygen released from the utilization device; and the flowmeter. The respective values of the oxygen consumption amount calculated from the oxygen flow rate detected by the oxygen concentration detector and the oxygen concentration detected by the concentration detector are processed, and the oxygen flow rate corresponding to the oxygen consumption amount is supplied based on the calculation result. A control device is provided for adjusting the pressurizing operation of the pressure pump so that the pressure is increased. An embodiment of the present invention will be described in detail below based on the drawings. FIG. 1 shows a system diagram of an embodiment in which the present invention is applied to a culture tank equipped with an oxygen concentrator. In the figure, on the inlet side of the nitrogen adsorption towers 1 and 2, which form the main body of the oxygen concentrator, there is a pressure pump 4 that pressurizes and supplies air sent from an inlet pipe 3 to a water droplet separator 5 and a valve 6. 8
are connected via. Further, the outlet sides of the nitrogen adsorption towers 1 and 2 are connected to an oxygen tank 12 via valves 10 and 11, respectively, and are led from there through an extraction pipe 13 to a culture tank 16 as an oxygen utilization device. There is. Others In the figure, 7 and 9 indicate exhaust valves of each adsorption tower 1 and 2. The culture tank 16 is provided with a supply port 15 through which concentrated oxygen supplied from the adsorption towers 1 and 2 is introduced, and an exhaust port 17 through which exhaust gas from the tank is discharged.
The supplied oxygen is diffused from a spargeer 20 installed below the culture solution 18, and then passed through an impeller 2.
1, it rises in the liquid while being stirred and is exhausted.
In the figure, 22 is a baffle plate, and 23 is an impeller rotation drive mechanism. In this embodiment, an electromagnetic flow meter 14 is provided to detect the flow rate of oxygen supplied between the take-out pipe 13 from the nitrogen adsorption towers 1 and 2 and the supply port 15 of the culture tank 16. Furthermore, a sensor 19 is installed in the exhaust port 17 of the culture tank 16 to detect the oxygen concentration in the exhausted exhaust gas. Detected electrical signals from the electromagnetic flowmeter 14 and oxygen concentration sensor 19 are electrically coupled to a control device 24, respectively. The control device 24 calculates the amount of oxygen consumed in the culture tank 16 based on the oxygen concentration detection signal from the sensor 19, and combines the calculated amount of oxygen consumed, that is, the data about the required amount of oxygen in the culture tank 16 with the above-mentioned data. It is equipped with a circuit that generates a control signal based on the data of the actual amount of oxygen supplied at each point in time detected by the flow meter 14. The control signal is electrically connected to the rotation speed variable control section of the pressure pump 4. The operation of the apparatus according to the embodiment of the present invention will be described below. First, the adsorption tower 1 is subjected to a pressure adsorption process, and the adsorption tower 2 is subjected to a depressurization process. For this purpose, valves 6, 9, 10 are opened and valves 7, 8, 11 are closed. By switching these valves, air from the feed pipe 3 is pressurized by the pressure pump 4, dehumidified by the water droplet separator 5, and then sent to the adsorption tower 1 via the valve 6. Adsorption tower 1
In this case, nitrogen in the pressurized air is selectively adsorbed, and oxygen is sent to an oxygen tank 12 through a valve 10.
Meanwhile, during this time, the adsorption tower 2 in the depressurization process is opened to the atmosphere by the valve 9, and the nitrogen adsorbed in the adsorption tower 2 in the previous cycle is exhausted to the outside of the system (operation cycle No. .1). Next, the adsorption tower 1 is switched to the depressurization exhaust process, and the adsorption tower 2 is switched to the pressure equalization process. In this case, valves 7 and 11 are opened and valves 6, 8, 9 and 10 are closed. By these valve switching operations, the adsorption tower 1 is opened to the atmosphere through the valve 7, and the nitrogen adsorbed in this adsorption tower is exhausted to the outside of the system. On the other hand, a part of the oxygen stored in the oxygen tank 12 is returned to the adsorption tower 2 through the valve 11 (operation cycle No. 2). Thereafter, each step is similarly repeated for adsorption towers 1 and 2 as operation cycles No. 3 and No. 4. This state is shown in the table below.
【表】
酸素タンク１２中の濃縮酸素は送入管１３を通
つて供給口１５から培養槽１６中に導入され、ス
パージヤ２０、インペラ２１、バツフル板２２で
微細な気泡に分散されて培養液１８中に散気さ
れ、ここで微生物の培養のためにその一部を消費
された後に排気口１７から排出される。
ここで本実施例中においては、供給口１５にお
ける供給酸素流量が電磁流量計１４で検知され各
時点での流量値の検知信号が制御装置２４に送ら
れる。一方、排気口１７からの排気中における酸
素濃度がセンサ１９によつて検出されこの検知信
号が制御装置２４に送られる。そして供給口１５
における供給酸素流量の検出値と排気中における
酸素濃度の検出値に基づいて培養槽内での消費酸
素量が算出される。制御装置２４は、消費酸素量
の算出値に基づいて、一定の所要酸素濃度下で利
用装置へ供給しなければならない供給酸素流量を
算出する。そしてこの算出された供給酸素流量と
所要酸素濃度とに基づいて、吸着塔へ送入する原
料空気の送入圧力を求める。この後、原料空気の
送入圧力についての制御信号を出力してこれを送
圧ポンプ４の回転制御部に送り、原料空気の送入
圧力を調整して利用装置への供給酸素流量を制御
する。すなわち、排気中の酸素濃度の検出値と供
給口１５における供給酸素流量の検出値によつて
培養槽１６中での消費酸素量が算出され、したが
つてそれに対応して必要となる供給酸素流量が算
出され、これに基づいて一定の所要酸素濃度下で
この供給酸素流量を与える空気の送入圧力が演算
され、この演算出力が制御信号として送圧ポンプ
４に送られる。送圧ポンプ４の回転数はこの制御
信号によつて変化され、これによつて吸着塔へ送
入される空気の送入圧力が調整され、各制御時点
での実際の酸素供給流量が所要の酸素負荷に対応
するように制御される。
ここで酸素供給流量が一定の酸素濃度下で空気
の送入圧力によつて制御される根拠は、差圧吸着
法の実施に際してこれらの間に一定の相関々係が
存在するという本発明者等の研究、実験の結果に
基づくものである。すなわち第２図に示すように
酸素濃縮装置に供給される空気の送入圧力Ｐをパ
ラメータにとると、酸素濃度Ｃ（グラフ縦軸）と
供給酸素流量Ｆ（グラフ横軸）との間には明らか
に一定の関連性が認められた。たとえば、図中、
圧力がP1，P2，…Pnの順に減少するにつれて酸
素濃度も減少し、またパラメータとしての圧力Ｐ
を一定にすると酸素流量Ｆの増加にともなつて酸
素濃度Ｃが減少する。
したがつて、酸素濃度Ｃを一定に保持しながら
酸素流量Ｆを変化させるためには圧力Ｐを制御す
れば良いことになる。たとえば、図中、圧力P1、
一定の所要酸素濃度C1および酸素流量F1の条件
で運転していた装置の酸素流量F1を、酸素負荷
の低下にともなつてF2に減少させるためにはP1
→Pnに調整すれば良い。
ここでまた第３図に示すように、送入圧力（横
軸上Ｐ）と加圧空気量（縦軸上Ｗ）との間には一
定の相関が認められるので、圧力P1をPnまで低
下させることにより加圧空気量はW1―W2だけ減
少され、かかる圧力調整を行なわない場合よりも
△Ｗだけ損失が低下し、またポンプ回転数の対応
する低下で電力コストとも節減される。
前記第１図の装置において、吸着塔１，２とし
てゼオライト5A型吸着剤を夫々１Kg、２Kg充填
した内径64mm、層高630mmの塔を用い、送入圧力
1.5〜３Kg／cm2・Ｇ、酸素濃度80％で運転したと
ころ、運転中の平均送入圧力は２Kg／cm2・Ｇであ
つた。送入圧力3.0Kg／cm2・Ｇおよび2.0Kg／cm2・
Ｇに対して加圧空気量は夫々160／minおよび
120／minであるところから、本実施例では常
時最大圧力3.0Kg／cm2・Ｇで運転する場合に比較
して25％の空気量の節減が得られた。
このように本実施例においては、吸着塔１，２
から供給される酸素量を電磁流量弁１４によつて
検出すると共に、培養槽１６からの排気中の酸素
濃度をセンサ１９で検出して、これらの検出値に
基づいて消費酸素量を算出し、該消費酸素量に基
づいて所要酸素濃度下で酸素利用装置へ供給しな
ければならない供給酸素流量を算出し、算出した
供給酸素流量と所要酸素濃度とに基づいて吸着塔
へ送入する空気の送入圧力を求め、この送入圧力
に対応する制御装置２４からの制御信号で送圧ポ
ンプ４の回転数を調整して空気の送入圧力を制御
するようになされているので、培養槽１６の酸素
消費負荷に応じて加圧空気量を調整しその節減を
計ることができる。したがつて本実施例によれ
ば、酸素負荷の変動によらず常に一定の空気送入
圧力で一定量の酸素を供給する場合に比較して加
圧空気量の損失を著しく低減し、また送圧ポンプ
の消費電力コストを低下させることができる。
尚本発明は前記実施例における培養槽の他、酸
素を利用する一般の装置に広く適用することがで
きる。
叙上のように本発明によれば酸素利用装置の酸
素負荷変動に対応して原料ガスの送入圧力を制御
することにより酸素供給量を制御し、それによつ
て原料としての加圧気体の無益な消費による損失
を著しく低下させることができる。[Table] Concentrated oxygen in the oxygen tank 12 is introduced into the culture tank 16 from the supply port 15 through the inlet pipe 13, and is dispersed into fine bubbles by the spargeer 20, impeller 21, and bubble plate 22, and becomes the culture solution 18. Aeration is diffused into the air, where a portion of the air is consumed for culturing microorganisms, and then exhausted from the exhaust port 17. In this embodiment, the flow rate of oxygen supplied at the supply port 15 is detected by the electromagnetic flowmeter 14, and a detection signal of the flow rate value at each point in time is sent to the control device 24. On the other hand, the oxygen concentration in the exhaust from the exhaust port 17 is detected by the sensor 19, and this detection signal is sent to the control device 24. and supply port 15
The amount of oxygen consumed in the culture tank is calculated based on the detected value of the supplied oxygen flow rate and the detected value of the oxygen concentration in the exhaust gas. The control device 24 calculates the flow rate of oxygen that must be supplied to the utilization device under a certain required oxygen concentration based on the calculated value of the consumed oxygen amount. Then, based on the calculated supply oxygen flow rate and required oxygen concentration, the feeding pressure of the raw material air to be fed into the adsorption tower is determined. After that, a control signal regarding the feeding pressure of raw material air is output and sent to the rotation control section of the pressure sending pump 4, and the feeding pressure of raw material air is adjusted to control the flow rate of oxygen supplied to the utilization equipment. . That is, the amount of oxygen consumed in the culture tank 16 is calculated based on the detected value of the oxygen concentration in the exhaust gas and the detected value of the supplied oxygen flow rate at the supply port 15, and the required supplied oxygen flow rate is calculated accordingly. is calculated, and based on this, the air supply pressure that provides this supplied oxygen flow rate under a constant required oxygen concentration is calculated, and the output of this calculation is sent to the pressure pump 4 as a control signal. The rotational speed of the pressure pump 4 is changed by this control signal, thereby adjusting the feeding pressure of air fed into the adsorption tower, and adjusting the actual oxygen supply flow rate at each control point to the required amount. Controlled to correspond to oxygen load. Here, the reason why the oxygen supply flow rate is controlled by the air supply pressure under a constant oxygen concentration is that the present inventors believe that there is a certain correlation between these when implementing the differential pressure adsorption method. It is based on the results of research and experiments. In other words, as shown in Fig. 2, if we take the inlet pressure P of air supplied to the oxygen concentrator as a parameter, there is a relationship between the oxygen concentration C (vertical axis of the graph) and the supplied oxygen flow rate F (horizontal axis of the graph). A certain degree of association was clearly observed. For example, in the figure,
As the pressure decreases in the order of P 1 , P 2 ,...Pn, the oxygen concentration also decreases, and the pressure P as a parameter
When constant, the oxygen concentration C decreases as the oxygen flow rate F increases. Therefore, in order to change the oxygen flow rate F while keeping the oxygen concentration C constant, it is sufficient to control the pressure P. For example, in the figure, pressure P 1 ,
In order to reduce the oxygen flow rate F 1 of a device operating under the conditions of constant required oxygen concentration C 1 and oxygen flow rate F 1 to F 2 as the oxygen load decreases, P 1 is required.
→ Just adjust it to Pn. Again, as shown in Fig. 3, there is a certain correlation between the inlet pressure (P on the horizontal axis) and the pressurized air amount (W on the vertical axis), so the pressure P 1 is reduced to Pn. By lowering the pressure, the pressurized air volume is reduced by W 1 - W 2 , resulting in lower losses by △W than without such pressure adjustment, and the corresponding reduction in pump speed also saves on electricity costs. . In the apparatus shown in Fig. 1, adsorption towers 1 and 2 are towers with an inner diameter of 64 mm and a bed height of 630 mm filled with 1 kg and 2 kg of zeolite 5A type adsorbent, respectively, and the feeding pressure is
When operating at 1.5 to 3 kg/cm 2 ·G and an oxygen concentration of 80%, the average feed pressure during operation was 2 kg/cm 2 ·G. Feed pressure 3.0Kg/cm 2・G and 2.0Kg/cm 2・
The pressurized air amount for G is 160/min and
120/min, in this example, a 25% reduction in air volume was obtained compared to when operating at a maximum pressure of 3.0 Kg/cm 2 ·G. In this way, in this embodiment, the adsorption towers 1 and 2
The amount of oxygen supplied from the culture tank 16 is detected by the electromagnetic flow valve 14, the oxygen concentration in the exhaust gas from the culture tank 16 is detected by the sensor 19, and the amount of oxygen consumed is calculated based on these detected values, The flow rate of supplied oxygen that must be supplied to the oxygen utilization device at the required oxygen concentration is calculated based on the amount of oxygen consumed, and the flow of air to the adsorption tower is calculated based on the calculated supplied oxygen flow rate and the required oxygen concentration. The air supply pressure is controlled by determining the input pressure and adjusting the rotation speed of the pressure pump 4 using a control signal from the control device 24 corresponding to this supply pressure. It is possible to adjust the amount of pressurized air according to the oxygen consumption load and measure savings. Therefore, according to this embodiment, the loss in the amount of pressurized air is significantly reduced compared to the case where a constant amount of oxygen is always supplied at a constant air supply pressure regardless of changes in the oxygen load, and the The power consumption cost of the pressure pump can be reduced. It should be noted that the present invention can be widely applied to general devices that utilize oxygen, in addition to the culture tank in the above-mentioned embodiments. As described above, according to the present invention, the amount of oxygen supplied is controlled by controlling the feeding pressure of the raw material gas in response to changes in the oxygen load of the oxygen utilization device, thereby reducing the uselessness of pressurized gas as a raw material. losses due to heavy consumption can be significantly reduced.
第１図は本発明の一実施例の概要を示す系統
図、第２図は酸素流量と酸素濃度との関係を示す
特性図、第３図は空気送入圧力と加圧空気量との
関係を示す特性図である。
１，２…吸着塔、４…送圧ポンプ、１４…電磁
流量計、１６…培養槽、１９…酸素濃度センサ、
２４…制御装置。
Fig. 1 is a system diagram showing an overview of an embodiment of the present invention, Fig. 2 is a characteristic diagram showing the relationship between oxygen flow rate and oxygen concentration, and Fig. 3 is a relationship between air supply pressure and pressurized air amount. FIG. 1, 2... Adsorption tower, 4... Pressure pump, 14... Electromagnetic flow meter, 16... Culture tank, 19... Oxygen concentration sensor,
24...Control device.
Claims (1)
合ガスを少なくともその中の一つの成分に対して
選択的な吸着性を有する吸着物質を含む吸着塔内
に加圧送入し、差圧吸着法により分離して濃縮さ
れた酸素を含むガスを生成し、これを酸素の利用
装置に一定の所要酸素濃度下で供給する方法にお
いて、 前記利用装置に供給される酸素流量および前記
利用装置から放出される酸素濃度を夫々検出し、
前記酸素濃度の検出値と前記酸素流量の検出値に
基づいて利用装置における酸素消費量を算出する
こと、 該酸素消費量に基づいて所要酸素濃度下で前記
利用装置に供給しなければならない供給酸素流量
を算出すること、 算出された該供給酸素流量と前記所要酸素濃度
とに基づいて前記吸着塔へ送入する混合ガスの送
入圧力を求めること、 求められた該送入圧力に基づいて前記吸着塔へ
送入する混合ガスの送入圧力を制御すること、 を特徴とする酸素の利用装置における酸素流量制
御方法。 ２ チツ素および酸素を主要な成分として含む混
合ガスを加圧送入する圧送ポンプ、前記混合ガス
中の少なくとも一つの成分に対して選択的な吸着
性を有する吸着物質で充填された吸着塔、および
前記吸着塔中で吸着工程および脱着工程を反復さ
せ差圧吸着法により濃縮された酸素を含むガスを
生成して供給するための切換制御系からなる酸素
濃縮装置を備えた酸素の利用装置において、前記
酸素濃縮装置から前記利用装置に供給される酸素
流量を検出する流量計と、前記利用装置から放出
される酸素濃度を検出する濃度検知器と、前記流
量計で検出された酸素流量および前記濃度検知器
で検出された酸素濃度から算出される酸素消費量
の夫々の値を演算処理し、この演算結果に基づい
て酸素消費量に対応する酸素流量が供給されるよ
うに前記圧送ポンプの加圧動作を調整する制御装
置とを備えたことを特徴とする酸素の利用装置に
おける酸素流量制御装置。[Scope of Claims] 1. A mixed gas containing nitrogen and oxygen as main components is fed under pressure into an adsorption tower containing an adsorption material that has selective adsorption properties for at least one of the components, A method of generating a gas containing concentrated oxygen by separating it by a differential pressure adsorption method and supplying it to an oxygen utilization device under a constant required oxygen concentration, the method comprising: Detect the oxygen concentration released from the device,
calculating an amount of oxygen consumed in the utilization device based on the detected value of the oxygen concentration and the detected value of the oxygen flow rate; calculating the flow rate; determining the feeding pressure of the mixed gas to be fed to the adsorption tower based on the calculated supply oxygen flow rate and the required oxygen concentration; 1. A method for controlling an oxygen flow rate in an oxygen utilization device, comprising: controlling the pressure at which a mixed gas is fed into an adsorption tower. 2. A pressure pump that feeds a mixed gas containing nitrogen and oxygen as main components under pressure, an adsorption tower filled with an adsorbent that has selective adsorption properties for at least one component in the mixed gas, and An oxygen utilization device comprising an oxygen concentrator comprising a switching control system for repeating the adsorption step and the desorption step in the adsorption tower to generate and supply a gas containing concentrated oxygen by a differential pressure adsorption method, a flow meter that detects the oxygen flow rate supplied from the oxygen concentrator to the utilization device; a concentration detector that detects the oxygen concentration released from the utilization device; and the oxygen flow rate and the concentration detected by the flow meter. Each value of the oxygen consumption amount calculated from the oxygen concentration detected by the detector is processed, and based on the calculation result, the pressure pump is pressurized so that the oxygen flow rate corresponding to the oxygen consumption amount is supplied. 1. An oxygen flow rate control device in an oxygen utilization device, comprising: a control device for adjusting operation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2795680A JPS56125206A (en) | 1980-03-07 | 1980-03-07 | Controlling method of oxygen flow rate in utilizing apparatus of oxygen and controlling apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2795680A JPS56125206A (en) | 1980-03-07 | 1980-03-07 | Controlling method of oxygen flow rate in utilizing apparatus of oxygen and controlling apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS56125206A JPS56125206A (en) | 1981-10-01 |
| JPS647001B2 true JPS647001B2 (en) | 1989-02-07 |
Family
ID=12235334
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2795680A Granted JPS56125206A (en) | 1980-03-07 | 1980-03-07 | Controlling method of oxygen flow rate in utilizing apparatus of oxygen and controlling apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS56125206A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100455680B1 (en) * | 2001-11-30 | 2004-11-06 | (주)바이오텔 | Apparatus for supplying oxygen |
| JP2013117346A (en) * | 2011-12-02 | 2013-06-13 | Osaka Gas Co Ltd | Industrial furnace apparatus |
-
1980
- 1980-03-07 JP JP2795680A patent/JPS56125206A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS56125206A (en) | 1981-10-01 |
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