JPH11333258A - Control of operating pressure in membrane separation process - Google Patents
Control of operating pressure in membrane separation processInfo
- Publication number
- JPH11333258A JPH11333258A JP14716498A JP14716498A JPH11333258A JP H11333258 A JPH11333258 A JP H11333258A JP 14716498 A JP14716498 A JP 14716498A JP 14716498 A JP14716498 A JP 14716498A JP H11333258 A JPH11333258 A JP H11333258A
- Authority
- JP
- Japan
- Prior art keywords
- pressure
- liquid
- membrane separation
- treated
- storage tank
- 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.)
- Granted
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、ラテックス濃縮、
コロイドシリカ濃縮、有価物回収、廃液処理、金属分
級、水道水濾過、活性汚泥処理等に有用な膜分離プロセ
スの操作圧力の制御方法に関する。The present invention relates to a latex concentrate,
The present invention relates to a method for controlling an operation pressure of a membrane separation process useful for colloidal silica concentration, valuable resource recovery, waste liquid treatment, metal classification, tap water filtration, activated sludge treatment, and the like.
【０００２】[0002]
【従来の技術および発明が解決しようとする課題】膜分
離装置では、加圧ポンプで被処理液を分離膜に供給し、
分離膜によりその被処理液は溶質が除去された透過液
と、溶質が濃縮された濃縮液とに分離される。このよう
な膜分離装置において操作圧力を制御するには、一般的
に、手動または自動の圧力調整弁により行われる。例え
ば、特開平１０−４３５５２号公報には、図８に示すよ
うな膜分離プロセスの操作圧力の制御方法が開示されて
いる。この公報に開示された発明は、５ＭＰａを超える
ような高圧域の制御を行う際に圧力調整弁への負担が大
きくなり、安定した圧力制御が困難になることがあるの
で、低圧域から高圧域までの任意の圧力で常に安定に制
御することが可能な膜分離プロセスの操作圧力の制御方
法を提供するものであり、以下に説明するような発明が
開示されている。すなわち、原液タンク２１に収容され
た原液は加圧送給ポンプ２２により分離膜モジュール２
３の原液入口２４に供給され、分離膜モジュール２３に
おいて、溶質が除かれた透過液と溶質が濃縮された濃縮
液とに分離され、透過液は透過液出口２５から排出さ
れ、濃縮液は濃縮液出口２６から管路２７に排出され
る。管路２７には、自動調圧弁２８およびオリフィス２
９が直列に配置されており、このオリフィス２９は、あ
る一定の流速、一定の溶液密度および粘度において、５
ＭＰａの圧力損失を発生する。オリフィス２９にはバイ
パス回路３０が設けられ、そのバイパス回路３０に仕切
弁３１が配置されている。上記のように構成される膜分
離プロセスにおいて、５ＭＰａまでの低圧域での圧力制
御を行う場合には、バイパス回路３０の仕切弁３１を開
くことによりオリフィス２９の効果が排除され、自動調
圧弁２８のみで圧力制御が行われる。一方、１０ＭＰａ
までの高圧域での圧力制御を行う場合には、バイパス回
路３０の仕切弁３１を閉じることによりオリフィス２９
で５ＭＰａの圧力損失を発生させ、残り５ＭＰａの圧力
が自動調圧弁２８で制御される。このように、上記公報
に記載された圧力制御方法は、操作圧力範囲を大小に分
けて、それぞれの圧力範囲において圧力を制御しようと
するものである。ところが、このような圧力制御方法で
は、膜分離装置において満足な膜分離ができないことが
ある。2. Description of the Related Art In a membrane separation apparatus, a liquid to be treated is supplied to a separation membrane by a pressure pump.
The liquid to be treated is separated by the separation membrane into a permeate from which the solute has been removed and a concentrate from which the solute has been concentrated. In such a membrane separation device, the operation pressure is generally controlled by a manual or automatic pressure regulating valve. For example, Japanese Patent Laid-Open Publication No. Hei 10-43552 discloses a method for controlling the operating pressure of the membrane separation process as shown in FIG. According to the invention disclosed in this publication, when controlling a high-pressure range exceeding 5 MPa, a load on a pressure regulating valve is increased, and stable pressure control may be difficult. The present invention provides a method for controlling the operating pressure of a membrane separation process that can always be stably controlled at an arbitrary pressure up to and including the invention described below. That is, the stock solution stored in the stock solution tank 21 is separated from the separation membrane module 2 by the pressurized feed pump 22.
3 and is separated into a permeate from which the solute has been removed and a concentrated solution in which the solute has been concentrated in the separation membrane module 23. The permeate is discharged from the permeate outlet 25, and the concentrate is concentrated. The liquid is discharged from a liquid outlet 26 to a conduit 27. An automatic pressure regulating valve 28 and an orifice 2
9 are arranged in series, the orifice 29 having a constant flow rate, a constant solution density and viscosity
A pressure loss of MPa occurs. A bypass circuit 30 is provided in the orifice 29, and a gate valve 31 is disposed in the bypass circuit 30. When performing pressure control in a low pressure range up to 5 MPa in the membrane separation process configured as described above, the effect of the orifice 29 is eliminated by opening the gate valve 31 of the bypass circuit 30, and the automatic pressure regulating valve 28. Pressure control is performed only by the pressure control. On the other hand, 10MPa
When the pressure control is performed in the high pressure range up to the orifice 29, the gate valve 31 of the bypass circuit 30 is closed to close the orifice 29.
Causes a pressure loss of 5 MPa, and the remaining pressure of 5 MPa is controlled by the automatic pressure regulating valve 28. As described above, the pressure control method described in the above publication divides the operating pressure range into large and small, and attempts to control the pressure in each pressure range. However, with such a pressure control method, satisfactory membrane separation may not be performed in the membrane separation apparatus.
【０００３】例えば、微小孔を有する透過性膜を備えた
クロスフロー型膜分離装置によりラテックスを濃縮する
場合、透過性膜により被処理ラテックスを透過成分と非
透過成分とに分離し、この非透過成分を再び膜分離装置
入側に供給して同じく透過性膜により透過成分と非透過
成分に分離し、同様の操作を繰り返すことによって非透
過成分の濃度を高めていく場合、操作圧力と、透過性膜
を透過する透過液の透過流束との関係は直線比例関係に
はなく、図２に示すような関係にある。図２において、
記号○、□、△、◇は、それぞれ、濃度１％、５％、１
０％、２０％を示す。図２に示すように、濃度１％の場
合、操作圧力約１０ｋｇ／ｃｍ2 までは、操作圧力と透
過流束は直線比例関係にあるが、それ以上に操作圧力が
大きくなっても、透過流束は増えない。また、濃度５
％、１０％、２０％の場合、透過流束と直線比例関係に
ある操作圧力の最大値は、それぞれ、約８ｋｇ／ｃ
ｍ2 、約４ｋｇ／ｃｍ2 、約２ｋｇ／ｃｍ2 である。上
記各濃度において、透過流束と直線比例関係にある最大
操作圧力以上の圧力を被処理液に加えても、透過流束は
ほとんど増えず、逆に膜表面にゲル層が形成されたり、
膜の流路が閉塞されるというような弊害が発生する可能
性がある。このように、被処理液の濃度によって適正な
操作圧力が変化する関係にある場合に、上記公報に記載
されたような圧力制御方法では、高い透過流束は得られ
ず、上記したような弊害が発生するだけである。For example, when the latex is concentrated by a cross-flow type membrane separation device having a permeable membrane having micropores, the latex to be treated is separated into a permeable component and a non-permeable component by the permeable membrane, and this non-permeable component is separated. When the components are supplied again to the inlet side of the membrane separation device and separated into permeate components and non-permeate components by the same permeable membrane, and the same operation is repeated to increase the concentration of the non-permeate components, the operation pressure and the permeation The relationship with the permeate flux of the permeate passing through the permeable membrane is not in a linear proportional relationship, but in a relationship as shown in FIG. In FIG.
The symbols ○, □, Δ, and Δ indicate concentrations of 1%, 5%, and 1%, respectively.
0% and 20% are shown. As shown in FIG. 2, when the concentration is 1%, the operating pressure and the permeation flux are linearly proportional up to the operation pressure of about 10 kg / cm 2. The bunch does not increase. In addition, the density 5
%, 10%, and 20%, the maximum value of the operating pressure, which is linearly proportional to the permeation flux, is about 8 kg / c, respectively.
m 2 , about 4 kg / cm 2 and about 2 kg / cm 2 . At each of the above concentrations, even if a pressure equal to or higher than the maximum operating pressure in a linear proportional relationship with the permeation flux is applied to the liquid to be treated, the permeation flux hardly increases, and conversely, a gel layer is formed on the membrane surface,
There is a possibility that an adverse effect such as blockage of the flow path of the membrane may occur. As described above, when there is a relationship in which the appropriate operation pressure changes depending on the concentration of the liquid to be treated, the pressure control method as described in the above publication cannot obtain a high permeation flux, and Only occurs.
【０００４】本発明は従来の技術の有するこのような問
題点に鑑みてなされたものであって、その目的は、透過
流束と直線比例関係にある操作圧力の最大値（最適操作
圧力）で操作しうるように、被処理液の濃度に応じて膜
分離装置に供給する被処理液の圧力を変化しうる膜分離
プロセスの操作圧力の制御方法を提供することにある。The present invention has been made in view of the above-mentioned problems of the prior art, and has as its object to determine the maximum value of the operating pressure (optimal operating pressure) which is linearly proportional to the permeation flux. An object of the present invention is to provide a method for controlling an operation pressure of a membrane separation process, which can change a pressure of a liquid to be treated supplied to a membrane separation apparatus according to a concentration of the liquid to be treated so as to be operable.
【０００５】[0005]
【課題を解決するための手段】上記目的を達成するため
に本発明の要旨は、被処理液貯留タンクに貯留した被処
理液を加圧して膜分離装置に供給し、この膜分離装置に
配置した透過性膜により被処理液を透過液と濃縮液に分
離し、透過液を系外に排出し、濃縮液を被処理液貯留タ
ンクに戻し、上記操作を繰り返して行うことにより濃縮
液の濃度を高める膜分離プロセスにおいて、被処理液の
濃度を測定し、その濃度における最適操作圧力で濾過操
作をしうるように、膜分離装置に供給される被処理液の
圧力を変化させることを特徴とする膜分離プロセスの操
作圧力の制御方法を第一の発明とし、上記第一の発明に
おいて、被処理液貯留タンクから膜分離装置に至る被処
理液送給経路に圧送手段と圧力計をこの順で配し、被処
理液貯留タンクまたは被処理液貯留タンクから膜分離装
置に至る被処理液送給経路に濃度計を配し、最適操作圧
力で操作しうるように、上記濃度計の指示により圧送手
段の圧力を変化させることを特徴とする膜分離プロセス
の操作圧力の制御方法を第二の発明とし、上記第一の発
明において、被処理液貯留タンクから膜分離装置に至る
被処理液送給経路に圧送手段と圧力計をこの順で配し、
被処理液貯留タンクまたは被処理液貯留タンクから膜分
離装置に至る被処理液送給経路に濃度計を配し、被処理
液送給経路の濃度計と圧力計の間に自動圧力調整弁を配
し、該自動圧力調整弁から被処理液貯留タンクに至るバ
イパス経路を設け、最適操作圧力で操作しうるように、
上記濃度計の指示により自動圧力調整弁の圧力を変化さ
せることを特徴とする膜分離プロセスの操作圧力の制御
方法を第三の発明とし、上記第一の発明において、被処
理液貯留タンクから膜分離装置に至る被処理液送給経路
に圧送手段と圧力計をこの順で配し、被処理液貯留タン
クまたは被処理液貯留タンクから膜分離装置に至る被処
理液送給経路に濃度計を配し、膜分離装置から被処理液
貯留タンクに至る濃縮液送給経路に自動圧力調整弁を配
し、最適操作圧力で操作しうるように、上記濃度計の指
示により自動圧力調整弁の圧力を変化させることを特徴
とする膜分離プロセスの操作圧力の制御方法を第四の発
明とし、上記第一の発明において、被処理液貯留タンク
から膜分離装置に至る被処理液送給経路に圧送手段と圧
力計をこの順で配し、被処理液貯留タンクまたは被処理
液貯留タンクから膜分離装置に至る被処理液送給経路に
濃度計を配し、被処理液送給経路の濃度計と圧力計の間
に自動圧力調整弁を配し、該自動圧力調整弁から被処理
液貯留タンクに至るバイパス経路を設け、さらに、膜分
離装置から被処理液貯留タンクに至る濃縮液送給経路に
自動圧力調整弁を配し、最適操作圧力で操作しうるよう
に、上記濃度計の指示により自動圧力調整弁の圧力を変
化させることを特徴とする膜分離プロセスの操作圧力の
制御方法を第五の発明とし、上記第二、第三、第四また
は第五の発明において、膜分離装置から透過液を排出す
る透過液排出経路に積算流量計を配し、以下の式により
算出される計算濃度を濃度計により測定された計測濃度
に代えて用いることを特徴とする膜分離プロセスの操作
圧力の制御方法を第六の発明とする。 計算濃度＝（被処理液の原液量×初期濃度）／（被処理
液の原液量−積算流量値） 以上のように構成される本発明によれば、被処理液の濃
度に適した最適操作圧力で膜分離を行うために、あらか
じめ被処理液の操作圧力と透過流束の関係について、濃
度をパラメーターとして、例えば、図２に示すような相
関図を求めておく。そして、その図を元にして、図３に
示すような濃度と最適操作圧力（透過流束と直線比例関
係にある操作圧力の最大値）の相関図を得る。そこで、
被処理液貯留タンクから膜分離装置に至る被処理液送給
経路に配した濃度計による計測濃度または積算流量計で
積算した透過液の流量より算出した計算濃度に応じて、
最適操作圧力で操作しうるように、膜分離装置に送給す
る被処理液の圧力を変化させることにより、効率的に膜
分離を行うことができる。In order to achieve the above object, the gist of the present invention is to pressurize a liquid to be treated stored in a liquid to be treated storage tank, supply the liquid to a membrane separation apparatus, and arrange the liquid in the membrane separation apparatus. The liquid to be treated is separated into a permeated liquid and a concentrated liquid by the permeable membrane, the permeated liquid is discharged out of the system, the concentrated liquid is returned to the liquid to be treated storage tank, and the concentration of the concentrated liquid is obtained by repeating the above operation. In the membrane separation process, the pressure of the liquid to be treated supplied to the membrane separation device is changed so that the concentration of the liquid to be treated is measured and the filtration operation can be performed at the optimum operating pressure at the concentration. The method for controlling the operating pressure of the membrane separation process to be performed is referred to as a first invention, and in the first invention, a pressure feeding means and a pressure gauge are provided in this order on a processing liquid supply path from the processing liquid storage tank to the membrane separation device. To the storage tank for the liquid to be treated. Arranges a concentration meter in the processing liquid supply path from the processing liquid storage tank to the membrane separation device, and changes the pressure of the pressure feeding means according to the instruction of the concentration meter so that the operation can be performed at the optimum operating pressure. The method for controlling the operation pressure of the membrane separation process is characterized by the second invention, and in the first invention, the pressure-feeding means and the pressure gauge are provided on the liquid-to-be-processed supply path from the liquid-to-be-processed storage tank to the membrane separation device. Arrange in this order,
A concentration meter is provided in the liquid supply path from the liquid storage tank or the liquid storage tank to the membrane separation device, and an automatic pressure regulating valve is provided between the concentration meter and the pressure gauge in the liquid supply path. To provide a bypass path from the automatic pressure control valve to the liquid storage tank to be processed, so that it can be operated at the optimum operation pressure,
The third invention provides a method for controlling the operating pressure of the membrane separation process, which comprises changing the pressure of the automatic pressure regulating valve according to the instruction of the concentration meter. A pressure-feeding means and a pressure gauge are arranged in this order in the liquid-to-be-processed supply path leading to the separation device, and a concentration meter is provided in the liquid-to-be-processed supply path from the liquid-to-be-processed storage tank or the liquid-to-be-processed storage tank to the membrane separation device. An automatic pressure regulating valve is arranged in the concentrated liquid supply path from the membrane separation device to the liquid storage tank to be treated, and the pressure of the automatic pressure regulating valve is instructed by the concentration meter so that the valve can be operated at the optimum operating pressure. The method for controlling the operation pressure of the membrane separation process is characterized in that the pressure is changed to a pressure in the processing liquid supply path from the processing liquid storage tank to the membrane separation device. Means and pressure gauge in this order , A concentration meter is provided in the liquid supply path from the liquid storage tank or the liquid storage tank to the membrane separation device, and an automatic pressure regulating valve is provided between the concentration meter and the pressure gauge in the liquid supply path. , A bypass path is provided from the automatic pressure control valve to the liquid storage tank, and an automatic pressure control valve is provided in the concentrated liquid supply path from the membrane separator to the liquid storage tank. As a fifth invention, a method for controlling the operation pressure of the membrane separation process, characterized in that the pressure of the automatic pressure control valve is changed by the instruction of the concentration meter so that the operation can be performed with the operation pressure, In the third, fourth or fifth invention, an integrated flow meter is disposed in a permeate discharge path for discharging the permeate from the membrane separation device, and the calculated concentration calculated by the following equation is measured by a concentration meter. Characterized in that it is used in place of The method of controlling the operating pressure of the release process to the sixth aspect of the present invention. Calculated concentration = (amount of undiluted solution of liquid to be treated × initial concentration) / (amount of undiluted solution of liquid to be treated−integrated flow value) According to the present invention configured as described above, an optimal operation suitable for the concentration of the liquid to be treated In order to perform membrane separation by pressure, for example, a correlation diagram as shown in FIG. 2 is obtained in advance with respect to the relationship between the operation pressure of the liquid to be treated and the permeation flux, using the concentration as a parameter. Then, based on the figure, a correlation diagram of the concentration and the optimum operation pressure (the maximum value of the operation pressure in a linear proportional relationship with the permeation flux) as shown in FIG. 3 is obtained. Therefore,
According to the concentration measured by the concentration meter arranged in the treatment liquid supply path from the treatment liquid storage tank to the membrane separation device or the concentration calculated from the flow rate of the permeate integrated by the integrating flow meter,
The membrane separation can be performed efficiently by changing the pressure of the liquid to be treated fed to the membrane separation device so that the operation can be performed at the optimum operation pressure.
【０００６】[0006]
【発明の実施の形態】以下に本発明の実施例を図面を参
照しながら説明する。図１は、第二の発明を適用するに
好適である膜分離プロセスの全体配置図である。図１に
おいて、１は被処理液１１を貯留する被処理液貯留タン
ク、２は濃度計、３はインバータ制御式の加圧送給ポン
プ、４は圧力計、５は透過性膜を備えた膜分離装置であ
り、被処理液貯留タンク１と膜分離装置５は被処理液送
給経路８で接続されている。なお、濃度計２は被処理液
貯留タンク１の中に配置することもできる。９は膜分離
装置５から透過液を排出する透過液排出経路である。膜
分離装置５から被処理液貯留タンク１には濃縮液送給経
路１０が形成されている。濃度計２には上記最適操作圧
力が入力されており、圧力計４で測定された圧力は濃度
計２にフィードバックされ、インバータ制御式の加圧送
給ポンプ３は、濃度計２と電気的に接続されている。そ
して、圧力計４で測定された圧力が最適操作圧力よりも
高ければ降圧するように、あるいは、最適操作圧力より
も低ければ昇圧するように、濃度計２からインバータ制
御式の加圧送給ポンプ３に対して指示が出される。Embodiments of the present invention will be described below with reference to the drawings. FIG. 1 is an overall layout diagram of a membrane separation process suitable for applying the second invention. In FIG. 1, 1 is a liquid storage tank for storing a liquid 11 to be processed, 2 is a concentration meter, 3 is a pressurized feed pump of an inverter control type, 4 is a pressure gauge, and 5 is a membrane separator having a permeable membrane. The treatment liquid storage tank 1 and the membrane separation device 5 are connected by a treatment liquid supply path 8. It should be noted that the concentration meter 2 can be disposed in the liquid storage tank 1 to be treated. 9 is a permeate discharge path for discharging the permeate from the membrane separation device 5. A concentrated liquid supply path 10 is formed from the membrane separation device 5 to the liquid storage tank 1 to be treated. The above-mentioned optimum operating pressure is input to the densitometer 2, and the pressure measured by the pressure gauge 4 is fed back to the densitometer 2, and the inverter-controlled pressurized feed pump 3 is electrically connected to the densitometer 2. Have been. The concentration meter 2 controls the pressure of the inverter-controlled pressurized feed pump 3 so as to decrease the pressure if the pressure measured by the pressure gauge 4 is higher than the optimum operating pressure, or to increase the pressure if the pressure measured is lower than the optimum operating pressure. Is instructed.
【０００７】膜分離装置５としては、一般的に使用され
ているもの（例えば、中空系膜を用いたもの）を使用す
ることもできるが、本出願人により出願された、膜分離
装置内に配置した透過性膜を水平面内の円周方向に微小
振幅で往復運動を行わせつつ被処理液を透過液と非透過
液に分離する装置を利用すれば、透過流束が大きく、膜
表面に目詰まりを起こすことなく、被処理液を高濃度ま
で濃縮することができるので、好ましい（例えば、特願
平１０−１１９１５３号参照）。As the membrane separation device 5, a commonly used one (for example, one using a hollow membrane) can be used. However, in the membrane separation device filed by the present applicant, By using a device that separates the liquid to be treated into a permeate and a non-permeate while reciprocating the arranged permeable membrane in the horizontal plane at a small amplitude in the circumferential direction, the permeation flux is large, This is preferable because the liquid to be treated can be concentrated to a high concentration without causing clogging (for example, see Japanese Patent Application No. 10-119153).
【０００８】以上のように構成される膜分離プロセスに
よれば、以下のようにして膜分離を行うことができる。According to the membrane separation process configured as described above, membrane separation can be performed as follows.
【０００９】まず、被処理液貯留タンク１に被処理液１
１を注入する。このとき、被処理液の容積を測定してお
く。そして、被処理液の初期濃度における操作圧力が最
適になるように、図３に基づく最適操作圧力で加圧送給
ポンプ３の運転を開始する。すると、被処理液は最適操
作圧力で経路８を経て膜分離装置５に送られる。その膜
分離装置５において膜分離された被処理液は、透過液と
濃縮液に分かれて、透過液は経路９より排出され、濃縮
液は経路１０を経て被処理液貯留タンク１に送給され
る。この膜分離プロセスにおける被処理液の濃度は、濃
度計２により測定されている。上記したように、インバ
ータ制御式の加圧送給ポンプ３は、濃度計２と電気的に
接続されており、濃度計２の指示を受けて作動すること
が可能である。First, the processing liquid 1 is stored in the processing liquid storage tank 1.
Inject 1. At this time, the volume of the liquid to be treated is measured. Then, the operation of the pressurized feed pump 3 is started at the optimum operation pressure based on FIG. 3 so that the operation pressure at the initial concentration of the liquid to be treated becomes optimum. Then, the liquid to be treated is sent to the membrane separation device 5 via the path 8 at the optimum operating pressure. The liquid to be treated which has been subjected to membrane separation in the membrane separation device 5 is separated into a permeate and a concentrate, and the permeate is discharged from the passage 9, and the concentrate is sent to the treatment liquid storage tank 1 via the passage 10. You. The concentration of the liquid to be treated in this membrane separation process is measured by the densitometer 2. As described above, the inverter-controlled pressurized feed pump 3 is electrically connected to the densitometer 2 and can operate in response to an instruction from the densitometer 2.
【００１０】被処理液貯留タンク１に戻された濃縮液は
経路８を経て膜分離装置５に送られるが、濃度計２にフ
ィードバックされた圧力計４の圧力がそのときの被処理
液の濃度における最適操作圧力よりも高い場合は、その
圧力を低くするように濃度計２からインバータ制御式の
加圧送給ポンプ３に信号が送られる。すなわち、インバ
ータ制御式の加圧送給ポンプ３から送給される被処理液
の圧力が降下する。逆に、濃度計２にフィードバックさ
れた圧力計４の圧力がそのときの被処理液の濃度におけ
る最適操作圧力よりも低い場合は、その圧力を高くする
ように濃度計２からインバータ制御式の加圧送給ポンプ
３に信号が送られる。すなわち、インバータ制御式の加
圧送給ポンプ３から送給される被処理液の圧力は上昇す
る。The concentrated liquid returned to the liquid storage tank 1 is sent to the membrane separation device 5 via the path 8, and the pressure of the pressure gauge 4 fed back to the concentration meter 2 indicates the concentration of the liquid to be treated at that time. If the pressure is higher than the optimum operation pressure in the above, a signal is sent from the concentration meter 2 to the inverter-controlled pressurized feed pump 3 so as to lower the pressure. That is, the pressure of the liquid to be treated, which is supplied from the inverter-controlled pressurized supply pump 3, drops. Conversely, if the pressure of the pressure gauge 4 fed back to the concentration meter 2 is lower than the optimal operating pressure at the concentration of the liquid to be treated at that time, the concentration meter 2 applies an inverter control type addition to increase the pressure. A signal is sent to the pressure feed pump 3. That is, the pressure of the liquid to be treated, which is supplied from the inverter-controlled pressurized supply pump 3, increases.
【００１１】図４は、第三の発明を適用するに好適であ
る膜分離プロセスの全体配置図である。図１と異なる点
は、被処理液送給経路８の濃度計２と圧力計４との間に
自動圧力調整弁１２が配置され、さらに、自動圧力調整
弁１２から被処理液貯留タンク１に至るバイパス経路１
３を設けた点にある。自動圧力調整弁１２は濃度計２と
電気的に接続されており、圧力計４で測定された圧力
が、最適操作圧力よりも高ければ降圧するように、ある
いは、最適操作圧力よりも低ければ昇圧するように、濃
度計２から自動圧力調整弁１２に対して指示が出され
る。FIG. 4 is an overall layout diagram of a membrane separation process suitable for applying the third invention. The difference from FIG. 1 is that an automatic pressure regulating valve 12 is arranged between the concentration meter 2 and the pressure gauge 4 in the liquid to be treated supply path 8, and furthermore, the automatic pressure regulating valve 12 is connected to the liquid to be treated storage tank 1. Bypass route 1
3 is provided. The automatic pressure regulating valve 12 is electrically connected to the concentration meter 2 so that the pressure measured by the pressure gauge 4 is decreased if the pressure is higher than the optimum operating pressure, or is increased if the pressure measured is lower than the optimum operating pressure. An instruction is issued from the densitometer 2 to the automatic pressure regulating valve 12 so as to perform the operation.
【００１２】以上のように構成される膜分離プロセス
は、図１の場合と同じように膜分離を行うことができ
る。すなわち、被処理液貯留タンク１内の濃縮液が経路
８を経て膜分離装置に送られるときに、濃度計２にフィ
ードバックされた圧力計４の圧力がそのときの被処理液
の濃度における最適操作圧力よりも高い場合は、その圧
力を低くするように濃度計２から自動圧力調整弁１２に
信号が送られる。その結果、自動圧力調整弁１２からバ
イパス経路１３を経て被処理液貯留タンク１に戻される
液量が増加されて経路８を流通する被処理液の圧力が降
下する。逆に、濃度計２にフィードバックされた圧力計
４の圧力がそのときの被処理液の濃度における最適操作
圧力よりも低い場合は、その圧力を高くするように濃度
計２から自動圧力調整弁１２に信号が送られる。その結
果、自動圧力調整弁１２からバイパス経路１３を経て被
処理液貯留タンク１に戻される液量が減少されて経路８
を流通する被処理液の圧力が上昇する。なお、第三の発
明で用いられる加圧送給ポンプ３は第二の発明のように
インバータ制御式のものを必ずしも用いる必要はなく、
定圧式ポンプ等を用いてもよい。In the membrane separation process configured as described above, membrane separation can be performed in the same manner as in FIG. That is, when the concentrated liquid in the liquid-to-be-treated storage tank 1 is sent to the membrane separation device via the path 8, the pressure of the pressure gauge 4 fed back to the concentration meter 2 indicates the optimal operation in the concentration of the liquid to be treated at that time. When the pressure is higher than the pressure, a signal is sent from the densitometer 2 to the automatic pressure control valve 12 so as to lower the pressure. As a result, the amount of liquid returned from the automatic pressure regulating valve 12 to the liquid storage tank 1 via the bypass path 13 is increased, and the pressure of the liquid to be processed flowing through the path 8 is reduced. Conversely, when the pressure of the pressure gauge 4 fed back to the concentration meter 2 is lower than the optimum operating pressure at the concentration of the liquid to be treated at that time, the automatic pressure control valve 12 from the concentration meter 2 increases the pressure. Is sent to As a result, the amount of liquid returned from the automatic pressure control valve 12 to the liquid storage tank 1 via the bypass path 13 is reduced, and the path 8
, The pressure of the liquid to be treated flowing increases. Note that the pressurized feed pump 3 used in the third invention is not necessarily required to be an inverter control type as in the second invention,
A constant pressure pump or the like may be used.
【００１３】図５は、第四の発明を適用するに好適であ
る膜分離プロセスの全体配置図である。図１と異なる点
は、膜分離装置５から被処理液貯留タンク１に至る濃縮
液送給経路１０に自動圧力調整弁７が配置された点にあ
る。自動圧力調整弁７は濃度計２と電気的に接続されて
おり、圧力計４で測定された圧力が最適操作圧力よりも
高ければ降圧するように、あるいは、最適操作圧力より
も低ければ昇圧するように、濃度計２から自動圧力調整
弁７に対して指示が出される。FIG. 5 is an overall layout diagram of a membrane separation process suitable for applying the fourth invention. The difference from FIG. 1 lies in that an automatic pressure regulating valve 7 is arranged in a concentrated liquid supply path 10 from the membrane separation device 5 to the liquid storage tank 1 to be treated. The automatic pressure regulating valve 7 is electrically connected to the concentration meter 2, and if the pressure measured by the pressure gauge 4 is higher than the optimum operating pressure, the pressure is reduced, or if the pressure is lower than the optimum operating pressure, the pressure is increased. Thus, the concentration meter 2 issues an instruction to the automatic pressure regulating valve 7.
【００１４】以上のように構成される膜分離プロセス
は、図１の場合と同じように膜分離を行うことができ
る。すなわち、被処理液貯留タンク１内の濃縮液が経路
８を経て膜分離装置に送られるときに、濃度計２にフィ
ードバックされた圧力計４の圧力がそのときの被処理液
の濃度における最適操作圧力よりも高い場合は、その圧
力を低くするように濃度計２から自動圧力調整弁７に信
号が送られる。その結果、自動圧力調整弁７から排出さ
れる濃縮液の圧力を低くするように弁７が調整される。
逆に、濃度計２にフィードバックされた圧力計４の圧力
がそのときの被処理液の濃度における最適操作圧力より
も低い場合は、その圧力を高くするように濃度計２から
自動圧力調整弁７に信号が送られる。その結果、自動圧
力調整弁７から排出される濃縮液の圧力を高くするよう
に弁７が調整される。なお、第四の発明で用いられる加
圧送給ポンプ３は第二の発明のようにインバータ制御式
のものを必ずしも用いる必要はなく、定圧式ポンプ等を
用いてもよい。In the membrane separation process configured as described above, membrane separation can be performed in the same manner as in FIG. That is, when the concentrated liquid in the liquid-to-be-treated storage tank 1 is sent to the membrane separation device via the path 8, the pressure of the pressure gauge 4 fed back to the concentration meter 2 indicates the optimal operation in the concentration of the liquid to be treated at that time. If the pressure is higher than the pressure, a signal is sent from the densitometer 2 to the automatic pressure control valve 7 to lower the pressure. As a result, the valve 7 is adjusted so that the pressure of the concentrated liquid discharged from the automatic pressure adjusting valve 7 is reduced.
Conversely, when the pressure of the pressure gauge 4 fed back to the concentration meter 2 is lower than the optimum operating pressure at the concentration of the liquid to be treated at that time, the automatic pressure control valve 7 is controlled by the concentration meter 2 to increase the pressure. Is sent to As a result, the valve 7 is adjusted so as to increase the pressure of the concentrate discharged from the automatic pressure adjusting valve 7. Note that the pressurized feed pump 3 used in the fourth invention does not necessarily need to be of an inverter control type as in the second invention, but may be a constant pressure pump or the like.
【００１５】図６は、第五の発明を適用するに好適であ
る膜分離プロセスの全体配置図である。図１と異なる点
は、被処理液送給経路８の濃度計２と圧力計４との間に
自動圧力調整弁１２が配置され、自動圧力調整弁１２か
ら被処理液貯留タンク１に至るバイパス経路１３を設け
た点と、膜分離装置５から被処理液貯留タンク１に至る
濃縮液送給経路１０に自動圧力調整弁７が配置された点
にある。自動圧力調整弁１２と７は濃度計２と電気的に
接続されており、圧力計４で測定された圧力が最適操作
圧力よりも高ければ降圧するように、あるいは、最適操
作圧力よりも低ければ昇圧するように、濃度計２から自
動圧力調整弁１２と７に対して指示が出され、上記した
プロセスに従って最適操作圧力で膜分離を行うことがで
きる。なお、第五の発明で用いられる加圧送給ポンプ３
は第二の発明のようにインバータ制御式のものを必ずし
も用いる必要はなく、定圧式ポンプ等を用いてもよい。FIG. 6 is an overall layout view of a membrane separation process suitable for applying the fifth invention. The difference from FIG. 1 is that an automatic pressure regulating valve 12 is disposed between the concentration meter 2 and the pressure gauge 4 in the liquid supply passage 8, and a bypass from the automatic pressure regulating valve 12 to the liquid storage tank 1 is provided. The point is that the path 13 is provided, and that the automatic pressure regulating valve 7 is disposed in the concentrated liquid supply path 10 from the membrane separation device 5 to the liquid storage tank 1 to be treated. The automatic pressure regulating valves 12 and 7 are electrically connected to the concentration meter 2 so that the pressure is reduced if the pressure measured by the pressure gauge 4 is higher than the optimum operating pressure, or if the pressure measured is lower than the optimum operating pressure. An instruction is issued from the densitometer 2 to the automatic pressure regulating valves 12 and 7 so as to increase the pressure, and the membrane separation can be performed at the optimum operating pressure according to the above-described process. The pressurized feed pump 3 used in the fifth invention
It is not always necessary to use an inverter control type as in the second invention, but a constant pressure pump or the like may be used.
【００１６】図７は、第六の発明を適用するに好適であ
る膜分離プロセスの全体配置図である。図１と異なる点
は、濃度計２がなく、被処理液送給経路８の加圧送給ポ
ンプ３と圧力計４との間に自動圧力調整弁１２が配置さ
れ、自動圧力調整弁１２から被処理液貯留タンク１に至
るバイパス経路１３を設けた点と、膜分離装置５から被
処理液貯留タンク１に至る濃縮液送給経路１０に自動圧
力調整弁７が配置された点と、透過液排出経路９に積算
流量計６を設けた点にある。積算流量計６には上記最適
操作圧力が入力されており、圧力計４で測定された圧力
は積算流量計６に入力され、積算流量計６はインバータ
制御式の加圧送給ポンプ３、自動圧力調整弁１２または
７と電気的に接続されている。そして、積算流量計６に
より積算された透過液の流量に基づいて上記した式に従
って被処理液の濃度が連続的に算出され、圧力計４で測
定された圧力がその計算濃度における最適操作圧力より
も高ければ降圧するように、あるいは、最適操作圧力よ
りも低ければ昇圧するように、積算流量計６から、それ
ぞれの機器（インバータ制御式の加圧送給ポンプ３、自
動圧力調整弁１２または７）に対して指示が出され、上
記したプロセスに従って最適操作圧力で膜分離を行うこ
とができる。すなわち、第六の発明は第二の発明から第
五の発明における濃度計２の代わりに積算流量計６によ
り被処理液の濃度を算出し、圧力操作をする方法であ
る。FIG. 7 is an overall layout diagram of a membrane separation process suitable for applying the sixth invention. The difference from FIG. 1 is that the concentration meter 2 is not provided, and the automatic pressure regulating valve 12 is disposed between the pressure supply pump 3 and the pressure gauge 4 in the liquid supply path 8 to be treated. A point in which a bypass path 13 leading to the processing liquid storage tank 1 is provided, a point in which the automatic pressure regulating valve 7 is disposed in the concentrated liquid supply path 10 from the membrane separation device 5 to the processing liquid storage tank 1, The point is that the integrating flow meter 6 is provided in the discharge path 9. The above-mentioned optimal operating pressure is input to the integrating flow meter 6, the pressure measured by the pressure gauge 4 is input to the integrating flow meter 6, and the integrating flow meter 6 is an inverter-controlled pressurized feed pump 3, an automatic pressure It is electrically connected to the regulating valve 12 or 7. Then, the concentration of the liquid to be treated is continuously calculated according to the above equation based on the flow rate of the permeated liquid integrated by the integrating flow meter 6, and the pressure measured by the pressure gauge 4 is calculated from the optimum operating pressure at the calculated concentration. If the pressure is too high, the pressure is reduced, or if the pressure is lower than the optimal operation pressure, the pressure is increased. The respective devices (inverter-controlled pressurized feed pump 3, automatic pressure regulating valve 12 or 7) are output from integrating flow meter 6. The membrane separation can be performed at the optimum operating pressure according to the above-described process. That is, the sixth invention is a method of calculating the concentration of the liquid to be treated by using the integrating flow meter 6 instead of the concentration meter 2 in the second invention to the fifth invention, and performing the pressure operation.
【００１７】かくして本発明によれば、常に最適操作圧
力で膜分離装置を運転することができるため、膜表面に
ゲル層が形成されることはなく、膜の流路が閉塞される
こともなく、極めて効率的に膜分離を行うことができる
とともに使用膜の長寿命化を図ることが可能である。ま
た、被処理液送給ポンプによる無駄な消費電力はないの
で、ランニングコストを低減することができる。例え
ば、無機質スラリー２００リッターを懸濁物の濃度を１
％から２０％に濃縮する場合に、図１に示すような構成
の限外濾過膜を用いた膜分離プロセスにおいて、定格容
量７．５ｋＷのインバータ制御式の加圧送給ポンプ３と
膜面積が１ｍ2 の膜分離装置５を用いて、最初から最後
まで操作圧力を１０ｋｇ／ｃｍ2 に固定した場合と、操
作圧力を図３に示すように変化させた場合における消費
電力を比較すると、後者のように操作圧力を変化させる
ことによって約４５％消費電力を節減することができ
た。なお、平均透過流束は、前者では５５Ｌ／ｍ2 ／hr
であり、後者では５４Ｌ／ｍ2／hrであった。Thus, according to the present invention, the membrane separation apparatus can always be operated at the optimum operating pressure, so that no gel layer is formed on the membrane surface and the flow path of the membrane is not blocked. In addition, the membrane separation can be performed extremely efficiently, and the life of the membrane to be used can be extended. In addition, there is no wasteful power consumption by the liquid supply pump, so that the running cost can be reduced. For example, 200 liters of an inorganic slurry is added to a suspension at a concentration of 1
When the concentration is reduced from 20% to 20%, in a membrane separation process using an ultrafiltration membrane configured as shown in FIG. 1, an inverter-controlled pressurized feed pump 3 having a rated capacity of 7.5 kW and a membrane area of 1 m The power consumption when the operating pressure was fixed at 10 kg / cm 2 from the beginning to the end using the membrane separation device 5 of Example 2 and the case where the operating pressure was changed as shown in FIG. 3 were compared. By changing the operating pressure, power consumption could be reduced by about 45%. The average permeation flux was 55 L / m 2 / hr for the former.
And in the latter case it was 54 L / m 2 / hr.
【００１８】[0018]
【発明の効果】本発明は上記のとおり構成されているの
で、膜表面にゲル層が形成されることはなく、膜の流路
が閉塞されることもなく、極めて効率的に膜分離を行う
ことができるとともに使用膜の長寿命化を図ることが可
能である。また、インバータ制御式の加圧送給ポンプを
用いた場合は、被処理液送給ポンプによる無駄な消費電
力はないので、ランニングコストを低減することができ
る。Since the present invention is constituted as described above, a gel layer is not formed on the membrane surface, the flow path of the membrane is not blocked, and the membrane is separated very efficiently. It is possible to extend the service life of the film to be used. In addition, when an inverter-controlled pressurized feed pump is used, there is no wasteful power consumption by the liquid-to-be-processed pump, so that the running cost can be reduced.
【図１】本発明の方法を適用するに好適である膜分離プ
ロセスの一実施形態の全体配置図である。FIG. 1 is a general layout of one embodiment of a membrane separation process suitable for applying the method of the present invention.
【図２】膜分離装置における操作圧力と透過流束の関係
を示す図である。FIG. 2 is a diagram showing the relationship between operating pressure and permeation flux in a membrane separation device.
【図３】膜分離装置における濃度と最適操作圧力の関係
を示す図である。FIG. 3 is a diagram showing a relationship between a concentration and an optimum operation pressure in the membrane separation device.
【図４】本発明の方法を適用するに好適である膜分離プ
ロセスの別の実施形態の全体配置図である。FIG. 4 is a general layout of another embodiment of a membrane separation process suitable for applying the method of the present invention.
【図５】本発明の方法を適用するに好適である膜分離プ
ロセスのさらに別の実施形態の全体配置図である。FIG. 5 is a general layout of yet another embodiment of a membrane separation process suitable for applying the method of the present invention.
【図６】本発明の方法を適用するに好適である膜分離プ
ロセスのさらに別の実施形態の全体配置図である。FIG. 6 is a general layout of yet another embodiment of a membrane separation process suitable for applying the method of the present invention.
【図７】本発明の方法を適用するに好適である膜分離プ
ロセスのさらに別の実施形態の全体配置図である。FIG. 7 is a general layout of yet another embodiment of a membrane separation process suitable for applying the method of the present invention.
【図８】従来の膜分離プロセスの一例の全体配置図であ
る。FIG. 8 is an overall layout view of an example of a conventional membrane separation process.
１…被処理液貯留タンク ２…濃度計 ３…加圧送給ポンプ ４…圧力計 ５…膜分離装置 ６…積算流量計 ７…自動圧力調整弁 ８…被処理液送給経路 ９…透過液排出経路 １０…濃縮液送給経路 １１…被処理液 １２…自動圧力調整弁 １３…バイパス経路 DESCRIPTION OF SYMBOLS 1 ... Liquid storage tank to be processed 2 ... Concentration meter 3 ... Pressure feed pump 4 ... Pressure gauge 5 ... Membrane separation device 6 ... Integrated flow meter 7 ... Automatic pressure control valve 8 ... Processing liquid supply path 9 ... Permeate discharge Path 10: Concentrated liquid supply path 11: Liquid to be treated 12: Automatic pressure regulating valve 13: Bypass path
───────────────────────────────────────────────────── フロントページの続き (72)発明者 榎本 正 兵庫県明石市大久保町高岡６丁目３−６ (72)発明者 島田 光重 兵庫県明石市魚住町住吉２−26−３−412 ──────────────────────────────────────────────────続 き Continued on the front page (72) Inventor Tadashi Enomoto 6-3-6 Takaoka, Okubo-cho, Akashi-shi, Hyogo (72) Inventor Mitsushige 2-26-3-412 Uozumi-cho, Sumiyoshi, Akashi-shi, Hyogo
Claims (6)
を加圧して膜分離装置に供給し、この膜分離装置に配置
した透過性膜により被処理液を透過液と濃縮液に分離
し、透過液を系外に排出し、濃縮液を被処理液貯留タン
クに戻し、上記操作を繰り返して行うことにより濃縮液
の濃度を高める膜分離プロセスにおいて、被処理液の濃
度を測定し、その濃度における最適操作圧力で濾過操作
をしうるように、膜分離装置に供給される被処理液の圧
力を変化させることを特徴とする膜分離プロセスの操作
圧力の制御方法。1. A liquid to be treated stored in a liquid to be treated storage tank is pressurized and supplied to a membrane separation device. The liquid to be treated is separated into a permeate and a concentrated solution by a permeable membrane arranged in the membrane separation device. Then, the permeate is discharged out of the system, the concentrated liquid is returned to the liquid storage tank, and the concentration of the liquid to be treated is measured in the membrane separation process in which the concentration of the concentrated liquid is increased by repeating the above operation. A method for controlling an operation pressure of a membrane separation process, wherein the pressure of a liquid to be treated supplied to a membrane separation device is changed so that a filtration operation can be performed at an optimum operation pressure at a concentration.
る被処理液送給経路に圧送手段と圧力計をこの順で配
し、被処理液貯留タンクまたは被処理液貯留タンクから
膜分離装置に至る被処理液送給経路に濃度計を配し、最
適操作圧力で操作しうるように、上記濃度計の指示によ
り圧送手段の圧力を変化させることを特徴とする請求項
１記載の膜分離プロセスの操作圧力の制御方法。2. A pressure supply means and a pressure gauge are arranged in this order on a liquid supply path from a liquid storage tank to a membrane separation apparatus to a liquid separation tank. 2. A membrane separation device according to claim 1, wherein a concentration meter is disposed in a liquid supply path leading to the processing liquid, and the pressure of the pressure-feeding means is changed by an instruction of the concentration meter so that the pressure can be operated at an optimum operation pressure. How to control the operating pressure of the process.
る被処理液送給経路に圧送手段と圧力計をこの順で配
し、被処理液貯留タンクまたは被処理液貯留タンクから
膜分離装置に至る被処理液送給経路に濃度計を配し、被
処理液送給経路の濃度計と圧力計の間に自動圧力調整弁
を配し、該自動圧力調整弁から被処理液貯留タンクに至
るバイパス経路を設け、最適操作圧力で操作しうるよう
に、上記濃度計の指示により自動圧力調整弁の圧力を変
化させることを特徴とする請求項１記載の膜分離プロセ
スの操作圧力の制御方法。3. A pressure supply means and a pressure gauge are arranged in this order on a liquid supply path from the liquid storage tank to the membrane separation device to the liquid separation tank, so that the liquid separation tank or the liquid separation tank is separated from the liquid separation tank. A concentration meter is arranged in the liquid supply path to be processed, and an automatic pressure regulating valve is arranged between the concentration meter and the pressure gauge in the liquid supply path to be treated, and from the automatic pressure regulating valve to the liquid storage tank to be treated. 2. The method according to claim 1, wherein a pressure of the automatic pressure regulating valve is changed by an instruction of the concentration meter so that a bypass path is provided so as to operate at an optimum operating pressure. .
る被処理液送給経路に圧送手段と圧力計をこの順で配
し、被処理液貯留タンクまたは被処理液貯留タンクから
膜分離装置に至る被処理液送給経路に濃度計を配し、膜
分離装置から被処理液貯留タンクに至る濃縮液送給経路
に自動圧力調整弁を配し、最適操作圧力で操作しうるよ
うに、上記濃度計の指示により自動圧力調整弁の圧力を
変化させることを特徴とする請求項１記載の膜分離プロ
セスの操作圧力の制御方法。4. A pressure-feeding means and a pressure gauge are arranged in this order in a liquid-to-be-processed supply path from the liquid-to-be-processed storage tank to the membrane separation device, and the liquid-to-be-processed storage tank or the liquid-to-be-processed storage tank is separated from the membrane separation device. A concentration meter is arranged in the liquid supply path to be processed up to, and an automatic pressure regulating valve is arranged in the concentrated liquid supply path from the membrane separation device to the liquid storage tank, so that it can be operated at the optimum operating pressure. 2. The method according to claim 1, wherein the pressure of the automatic pressure control valve is changed according to an instruction from the concentration meter.
る被処理液送給経路に圧送手段と圧力計をこの順で配
し、被処理液貯留タンクまたは被処理液貯留タンクから
膜分離装置に至る被処理液送給経路に濃度計を配し、被
処理液送給経路の濃度計と圧力計の間に自動圧力調整弁
を配し、該自動圧力調整弁から被処理液貯留タンクに至
るバイパス経路を設け、さらに、膜分離装置から被処理
液貯留タンクに至る濃縮液送給経路に自動圧力調整弁を
配し、最適操作圧力で操作しうるように、上記濃度計の
指示により自動圧力調整弁の圧力を変化させることを特
徴とする請求項１記載の膜分離プロセスの操作圧力の制
御方法。5. A processing liquid supply path from a liquid storage tank to be processed to a membrane separation device, a pressure feeding means and a pressure gauge are arranged in this order, and the processing liquid storage tank or the processing liquid storage tank is connected to the membrane separation device. A concentration meter is arranged in the liquid supply path to be processed, and an automatic pressure regulating valve is arranged between the concentration meter and the pressure gauge in the liquid supply path to be treated, and from the automatic pressure regulating valve to the liquid storage tank to be treated. An automatic pressure regulating valve is provided in the concentrated liquid supply path from the membrane separation device to the liquid storage tank to be treated, and the automatic concentration control valve is automatically operated according to the instruction of the concentration meter so that the operation can be performed at the optimum operation pressure. 2. The method according to claim 1, wherein the pressure of the pressure regulating valve is changed.
排出経路に積算流量計を配し、以下の式により算出され
る計算濃度を濃度計により測定された計測濃度に代えて
用いることを特徴とする請求項２、３、４または５記載
の膜分離プロセスの操作圧力の制御方法。 計算濃度＝（被処理液の原液量×初期濃度）／（被処理
液の原液量−積算流量値）6. An integrated flow meter is provided in a permeate discharge path for discharging a permeate from a membrane separation device, and the calculated concentration calculated by the following equation is used in place of the measured concentration measured by the densitometer. The method for controlling an operating pressure of a membrane separation process according to claim 2, 3, 4, or 5. Calculated concentration = (Amount of stock solution of liquid to be treated x Initial concentration) / (Amount of stock solution of liquid to be treated-integrated flow value)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14716498A JP4137231B2 (en) | 1998-05-28 | 1998-05-28 | Method for controlling the operating pressure of a membrane separation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14716498A JP4137231B2 (en) | 1998-05-28 | 1998-05-28 | Method for controlling the operating pressure of a membrane separation process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH11333258A true JPH11333258A (en) | 1999-12-07 |
| JP4137231B2 JP4137231B2 (en) | 2008-08-20 |
Family
ID=15424043
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP14716498A Expired - Fee Related JP4137231B2 (en) | 1998-05-28 | 1998-05-28 | Method for controlling the operating pressure of a membrane separation process |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP4137231B2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2005093053A1 (en) * | 2004-03-29 | 2005-10-06 | Fuji Photo Film Co., Ltd. | Method and apparatus of automatically isolating and purifying nucleic acid |
| WO2010061666A1 (en) * | 2008-11-27 | 2010-06-03 | 三菱重工業株式会社 | Multi-stage seawater desalination equipment and operation control method for multi-stage seawater desalination equipment |
-
1998
- 1998-05-28 JP JP14716498A patent/JP4137231B2/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2005093053A1 (en) * | 2004-03-29 | 2005-10-06 | Fuji Photo Film Co., Ltd. | Method and apparatus of automatically isolating and purifying nucleic acid |
| US7811758B2 (en) | 2004-03-29 | 2010-10-12 | Fujifilm Corporation | Method and apparatus of automatically isolating and purifying nucleic acid |
| WO2010061666A1 (en) * | 2008-11-27 | 2010-06-03 | 三菱重工業株式会社 | Multi-stage seawater desalination equipment and operation control method for multi-stage seawater desalination equipment |
| US8685249B2 (en) | 2008-11-27 | 2014-04-01 | Mitsubishi Heavy Industries, Ltd. | Multi-stage seawater desalination apparatus and operation control method of multi-stage seawater desalination apparatus |
Also Published As
| Publication number | Publication date |
|---|---|
| JP4137231B2 (en) | 2008-08-20 |
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