JPH0380920A - Membrane separation apparatus - Google Patents
Membrane separation apparatusInfo
- Publication number
- JPH0380920A JPH0380920A JP21936889A JP21936889A JPH0380920A JP H0380920 A JPH0380920 A JP H0380920A JP 21936889 A JP21936889 A JP 21936889A JP 21936889 A JP21936889 A JP 21936889A JP H0380920 A JPH0380920 A JP H0380920A
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- chamber
- liquid chamber
- cooling
- treated
- 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
- 239000012528 membrane Substances 0.000 title claims abstract description 36
- 238000000926 separation method Methods 0.000 title claims abstract description 13
- 239000007788 liquid Substances 0.000 claims abstract description 122
- 238000001816 cooling Methods 0.000 claims abstract description 40
- 238000010438 heat treatment Methods 0.000 claims abstract description 10
- 239000002826 coolant Substances 0.000 claims description 6
- 238000011144 upstream manufacturing Methods 0.000 claims description 6
- 230000006866 deterioration Effects 0.000 abstract description 5
- 238000005192 partition Methods 0.000 abstract description 4
- 230000002542 deteriorative effect Effects 0.000 abstract 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 25
- 239000002699 waste material Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 239000012466 permeate Substances 0.000 description 2
- 230000005494 condensation Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 239000012809 cooling fluid Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、純水製造や各種の排液濃縮に用いられる膜分
離装置で、詳しくは、液室と気室とに内部が仕切られた
分離器を設け、その分離器の前記液室に被処理液を供給
するための給液路と、前記液室を気室よりも高温にする
ための温度調整手段とを設け、前記分離器の仕切りに、
液室と気室との温度差に相当する水蒸気分圧差をもって
液室から気室に水蒸気のみを選択的に透過させる透過膜
を設けてある膜分離装置に関する。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a membrane separation device used for producing pure water and concentrating various waste liquids. A separator is provided, a liquid supply path for supplying the liquid to be treated to the liquid chamber of the separator, and a temperature adjustment means for making the liquid chamber higher than the air chamber, and In the partition,
The present invention relates to a membrane separation device provided with a permeable membrane that selectively transmits only water vapor from the liquid chamber to the air chamber with a water vapor partial pressure difference corresponding to the temperature difference between the liquid chamber and the air chamber.
従来の膜分離装置としては、第３図に示すように、前記
給液路（２）に、被処理液（純水製造では原水であり、
排液濃縮では排液である。）を冷却材として前記分離器
（１）の気室（１ｂ）を冷却する冷却部（２Ａ）を設け
、その給液路（２）のうち冷却部（２Ａ）から分離器（
１〉の液室（１ａ）に到る部分に、ボイラ等で製造され
た高温の加熱流体（水等）との熱交換により被処理液を
加熱する熱交換器（Ｈｌ）や電熱ヒータを設けて、前述
した温度調整手段を構成したものが知られている（例え
ば特公昭４９−４５４６１号公報や特開昭６０−１１８
２０４号公報）。また、第４図に示すように、前記の構
成に加え、前記給液路（２）のうち冷却部（２Ａ）より
も上流側の箇所に、冷水等の冷却用流体との熱交換によ
り被処理液を冷却する熱交換器（Ｈ２）を設けて、気室
（１ｂ）の冷却、液室（１ａ）の加熱を行うようにした
ものも知られている。As shown in FIG. 3, in a conventional membrane separation device, the liquid to be treated (raw water in pure water production) is connected to the liquid supply path (2).
In waste liquid concentration, it is waste liquid. ) is provided as a coolant to cool the air chamber (1b) of the separator (1).
A heat exchanger (Hl) and an electric heater are installed in the part leading to the liquid chamber (1a) of 1>, which heats the liquid to be treated by heat exchange with a high-temperature heating fluid (water, etc.) produced in a boiler etc. There are known devices in which the above-mentioned temperature adjustment means is configured (for example, Japanese Patent Publication No. 49-45461 and Japanese Patent Application Laid-Open No. 60-118).
Publication No. 204). In addition to the above configuration, as shown in FIG. 4, a portion of the liquid supply path (2) upstream of the cooling section (2A) is exposed to heat exchange with a cooling fluid such as cold water. There is also known a device in which a heat exchanger (H2) for cooling the processing liquid is provided to cool the air chamber (1b) and heat the liquid chamber (1a).
なお、（ＬＡ）が透過膜であり、（４）は、分離器（１
）の液室（１ａ）から排出される濃縮液を給液路（２）
に戻すブロー（４ａ）付の戻り路である。In addition, (LA) is a permeable membrane, and (4) is a separator (1
) The concentrated liquid discharged from the liquid chamber (1a) is transferred to the liquid supply path (2).
This is a return path with a blow (4a) that returns to
しかし、前記従来技術によるときは、次のような欠点が
あった。However, the prior art has the following drawbacks.
前者の従来技術によるときは、給液路における冷却部に
冷却材として供給される被処理液が常温で、その常温の
被処理液を熱交換器で加熱された液室内の高温被処理液
との温度差が、水蒸気の膜透過の駆動力となる液室と気
室との温度差となるため、十分な駆動力を得ることがで
きる温度差とするためには、液室内を高温にするか、或
いは、被処理液として低温のものを用意するかのいずれ
かが必要である。そして、前者の場合には、透過膜の早
期劣化を招来し、後者の場合には適用性に欠ける。In the former conventional technology, the liquid to be treated is supplied as a coolant to the cooling section in the liquid supply path at room temperature, and the liquid to be treated at room temperature is mixed with the high temperature liquid in the liquid chamber heated by a heat exchanger. The temperature difference between the liquid chamber and the air chamber is the driving force for water vapor permeation through the membrane, so in order to create a temperature difference that can provide sufficient driving force, it is necessary to raise the temperature inside the liquid chamber. Alternatively, it is necessary to prepare a low-temperature liquid as the liquid to be treated. The former case causes early deterioration of the permeable membrane, and the latter case lacks applicability.
他方、後者従来技術によるときは、冷却部に冷却材とし
て供給する被処理水を冷却するため、液室と気室との温
度を十分に確保しながらも、液室の低温化を図って透過
膜の早期劣化を防止でき、しかも、汎用性を向上できる
ものの、被処理水の冷却にエネルギーが必要で、かつ、
−旦冷却した被処理水を加熱する必要があって加熱に対
する負荷が大きく加熱に大エネルギーが必要であること
によって、ランニングコストが高く付いていた。特に、
戻り路を設けて液を循環させることにより濃縮度を上げ
る場合、図中実線で示すように冷却用の熱交換器よりも
上流側に濃縮液を戻すようにすると、その冷却用の熱交
換器による冷却負荷が増大する。また、図中二点鎖線で
示すように冷却部と加熱用の熱交換器との間に濃縮液を
戻すようにすると、冷却された被処理水の冷却部への供
給量が著しく減少して、気室の冷却不足を招来し、その
結果、温度差確保のために液室内の高温化が不可避とな
って、透過膜の早期劣化を招来する。On the other hand, when using the latter conventional technology, in order to cool the water to be treated that is supplied as a coolant to the cooling section, while ensuring sufficient temperature between the liquid chamber and the air chamber, the temperature of the liquid chamber is lowered and the water permeates through the water. Although it can prevent early deterioration of the membrane and improve versatility, it requires energy to cool the water to be treated, and
- Since it is necessary to heat the water to be treated which has been cooled, the heating load is large and a large amount of energy is required for heating, resulting in high running costs. especially,
When increasing the concentration by providing a return path and circulating the liquid, as shown by the solid line in the figure, if the concentrated liquid is returned upstream from the cooling heat exchanger, the cooling heat exchanger cooling load increases. In addition, if the concentrated liquid is returned between the cooling section and the heating heat exchanger as shown by the two-dot chain line in the figure, the amount of cooled water to be treated that is supplied to the cooling section will be significantly reduced. This results in insufficient cooling of the air chamber, and as a result, the temperature inside the liquid chamber inevitably increases to ensure a temperature difference, leading to early deterioration of the permeable membrane.
本発明の目的は、上記従来欠点を解消する点にある。An object of the present invention is to eliminate the above-mentioned conventional drawbacks.
本発明による膜分離装置の特徴構成は、前記温度調整手
段を構成するに、ヒートポンプを設け、そのヒートポン
プの凝縮器と蒸発器とのうち、凝縮器を液室加熱源とし
、かつ、蒸発器を気室冷却源として夫々設けてある点に
ある。The characteristic structure of the membrane separation apparatus according to the present invention is that a heat pump is provided to constitute the temperature adjustment means, and of a condenser and an evaporator of the heat pump, the condenser is used as a liquid chamber heating source, and the evaporator is used as a heat source for the liquid chamber. The point is that each is provided as a cooling source for the air chamber.
前記給液路に被処理液を冷却材として前記気室を冷却す
る冷却部を設け、その給液路のうち冷却部よりも上流側
の部分に、被処理液の冷却器として前記蒸発器を設け、
冷却部から前記液室に到る部分に、被処理液の加熱器と
して前記凝縮器を設けてあることが好ましい。A cooling unit is provided in the liquid supply path to cool the air chamber using the liquid to be treated as a coolant, and the evaporator is provided as a cooler for the liquid to be treated in a portion of the liquid supply path upstream of the cooling unit. established,
It is preferable that the condenser is provided as a heater for the liquid to be treated in a portion extending from the cooling section to the liquid chamber.
更に、前記分離器の液室から排出される濃縮液を前記給
液路に戻すための戻り路を設けることが好ましい。Furthermore, it is preferable to provide a return path for returning the concentrated liquid discharged from the liquid chamber of the separator to the liquid supply path.
分離器の気室は、ヒートポンプの蒸発器による吸熱作用
によって冷却される。他方、液室は、ヒートポンプの凝
縮による放熱作用によって加熱される。従って、液室と
気室との温度差として、水蒸気の膜透過に十分な温度差
を確保しながらも、液室の交換化を回避できる。The air chamber of the separator is cooled by the endothermic action of the evaporator of the heat pump. On the other hand, the liquid chamber is heated by the heat dissipation effect due to condensation of the heat pump. Therefore, it is possible to avoid replacing the liquid chamber while ensuring a temperature difference between the liquid chamber and the air chamber that is sufficient for water vapor to permeate through the membrane.
しかも、凝縮器と蒸発器とが１つのヒートポンプのもの
で、液室の加熱により凝縮器で得た冷熱を、外部に放出
することなく蒸発器での気室の冷却に利用するため、加
熱、冷却のための熱損失を少なくできる。Moreover, the heat pump has a single condenser and evaporator, and the cold heat obtained in the condenser by heating the liquid chamber is used to cool the air chamber in the evaporator without being released to the outside. Heat loss for cooling can be reduced.
特に、液室から放出される濃縮液を給液路に戻す場合は
、凝縮器により被処理液に付与した温熱を回収して熱効
率を向上できると共に、液の濃縮の場合、濃縮度を上げ
ることができる。In particular, when returning the concentrated liquid discharged from the liquid chamber to the liquid supply path, the thermal efficiency can be improved by recovering the heat imparted to the liquid to be treated using the condenser, and when concentrating the liquid, the degree of concentration can be increased. I can do it.
従って、本発明によれば、透過膜の早期劣化を招来する
ことなく、低コストで膜分離を行えるようになった。特
に請求項３記載のようにすれば、より一層コストの低下
を図れると共に、液の濃縮に好適である。Therefore, according to the present invention, membrane separation can be performed at low cost without causing early deterioration of the permeable membrane. Particularly, if the method described in claim 3 is adopted, the cost can be further reduced and it is suitable for concentrating the liquid.
次に本発明の実施例を示す。 Next, examples of the present invention will be shown.
膜分離装置は第１図に示すように、分離用の膜モジュー
ル（Ｍ）と、その膜モジュール（Ｍ）に被処理液を供給
するための給液路（２）と、温度調整手段とを備えてい
る。As shown in FIG. 1, the membrane separation apparatus includes a membrane module (M) for separation, a liquid supply path (2) for supplying the liquid to be treated to the membrane module (M), and temperature adjustment means. We are prepared.
前記膜モジュール（Ｍ）は、容器の内部を液室（１ａ）
と気室（１ｂ）と冷却室（ｌｃ）との３つに、気室（１
ｂ）に液室（１ａ）と冷却室（１ｃ）とが隣合う状態に
仕切り、液室（１ａ）と気室（１ｂ）との仕切りとして
、液室（１ａ）と気室（１ｂ）との温度差に相当する水
蒸気分圧差をもって高温側から低温側に水蒸気のみを透
過させる透過膜（ＬＡ）を設け、前記気室（１ｂ）と冷
却室（ｌｃ）との仕切りとして、伝熱板（ＩＢ）を設け
たものである。The membrane module (M) has a liquid chamber (1a) inside the container.
air chamber (1b), cooling chamber (lc), and air chamber (1b);
b) is partitioned so that the liquid chamber (1a) and the cooling chamber (1c) are adjacent to each other, and as a partition between the liquid chamber (1a) and the air chamber (1b), A permeable membrane (LA) that allows only water vapor to pass from the high temperature side to the low temperature side with a water vapor partial pressure difference corresponding to the temperature difference of is provided, and a heat transfer plate (LA) is provided as a partition between the air chamber (1b) and the cooling chamber (lc) IB).
前記給液路（２）の途中は、前記膜モジュール（Ｍ）の
冷却室（１ｃ）から構成されている。つまり、給液路（
２）は、冷却室（ＩＣ）と伝熱板（ＩＢ）とから被処理
液を冷却材として前記気室（１ｂ）を冷却するように構
成された冷却部（２Ａ）を備えており、膜モジュール（
Ｍ）は、液室（１ａ）・気室（１ｂ）・透過膜（１Ａ）
からなる分離器（１）と前記冷却部（２Ａ）とを一体化
したものである。The middle of the liquid supply path (2) is constituted by a cooling chamber (1c) of the membrane module (M). In other words, the liquid supply path (
2) is equipped with a cooling section (2A) configured to cool the air chamber (1b) by using the liquid to be treated from a cooling chamber (IC) and a heat exchanger plate (IB) as a coolant; module(
M) includes liquid chamber (1a), air chamber (1b), and permeable membrane (1A).
The separator (1) and the cooling section (2A) are integrated.
前記温度調整手段は、前記膜モジュール（Ｍ）の液室（
１ａ）を気室（１ｂ）よりも高温にして、液室（１ａ）
から気室（１，ｂ）に水蒸気を透過膜（１Ａ）を通して
透過させる手段である。具体的には、圧縮機（３Ａ）・
凝縮器（３Ｂ）・膨張弁（３Ｃ）・蒸発器（３Ｄ）・圧
縮機（３Ａ）とその記載順に冷媒を循環させることによ
り、凝縮器（３Ｂ）で放熱を、かつ、蒸発器（３Ｄ）で
吸熱を夫々行う１つのヒートポンプ（３）を設け、その
ヒートポンプ（３）の凝縮器（３Ｂ）を、前記給液路（
２）のうち冷却室（ＩＣ）から液室（１ａ）に到る部分
に被処理液の加熱器として設け、前記蒸発器（３Ｄ）を
、給液路（２）のうち冷却室（ＩＣ）よりも上流側の部
分に被処理液の冷却器として設けたものがある。つまり
、凝縮器（３Ｂ）を加熱源として、液室（１ａ）に供給
する被処理液を加熱することにより液室（１ａ）を間接
的に加熱し、蒸発器（３Ｄ）を冷却源として、冷却室（
ｌｃ）に供給する被処理液を冷却することにより気室（
１ｂ）を間接的に冷却するものである。The temperature adjustment means includes a liquid chamber (
1a) to a higher temperature than the air chamber (1b), and the liquid chamber (1a)
This is a means for permeating water vapor from the air chamber (1, b) through the permeable membrane (1A). Specifically, the compressor (3A)
By circulating the refrigerant in the order listed in the condenser (3B), expansion valve (3C), evaporator (3D), and compressor (3A), the condenser (3B) releases heat and the evaporator (3D) One heat pump (3) is provided, and the condenser (3B) of the heat pump (3) is connected to the liquid supply path (
2), the portion from the cooling chamber (IC) to the liquid chamber (1a) is provided as a heater for the liquid to be treated, and the evaporator (3D) is installed in the portion extending from the cooling chamber (IC) to the liquid chamber (1a) in the liquid supply path (2). There is a device installed as a cooler for the liquid to be treated at a portion upstream of the wafer. In other words, the liquid chamber (1a) is indirectly heated by using the condenser (3B) as a heat source to heat the liquid to be treated that is supplied to the liquid chamber (1a), and the evaporator (3D) is used as a cooling source. Cooling room (
The air chamber (
1b) is indirectly cooled.
かつ、膜分離装置は、前記給液路（２）のうち蒸発器（
３Ｄ）よりも上流側の部分に前記液室（１ａ）から排出
される濃縮液を戻すためのブロー（４ａ）付きの戻り路
（４）を備えている。In addition, the membrane separator includes an evaporator (
A return path (4) with a blow (4a) for returning the concentrated liquid discharged from the liquid chamber (1a) is provided in a portion upstream of the liquid chamber (1a).
上記の如く構成された膜分離装置は、純水製造や排液の
濃縮に用いられるのであって、純水製造時の被処理液は
原水であり、排液濃縮時の被処理は排液である。The membrane separator configured as described above is used for producing pure water and concentrating wastewater, and when producing pure water, the liquid to be treated is raw water, and when concentrating wastewater, the liquid to be treated is wastewater. be.
上記の膜分離装置によれば、液室（１ａ）から気室（１
ｂ）への透過膜（１Ａ）を通しての水蒸気の透過により
液室（１ａ）内の被処理液が濃縮される。この濃縮液は
被処理液に戻されて循環するため、時間経過に伴って濃
縮度が次第に高くなる。他方、気室（１ｂ）内に透過し
た水蒸気は、冷却によって結露し、純水として排出され
る。そして、被処理液の加熱により凝縮器（３Ｂ）で生
成された冷熱は、ヒートポンプ（３）で蒸発器（３Ｄ）
に運ばれて、冷却部（２Ａ）へ供給する被処理液の冷却
に利用されるため、冷熱の無駄がない。According to the above membrane separator, from the liquid chamber (1a) to the air chamber (1a).
b) The liquid to be treated in the liquid chamber (1a) is concentrated by permeation of water vapor through the permeable membrane (1A). Since this concentrated liquid is returned to the liquid to be treated and circulated, the degree of concentration gradually increases as time passes. On the other hand, the water vapor that has permeated into the air chamber (1b) is condensed by cooling and is discharged as pure water. The cold energy generated in the condenser (3B) by heating the liquid to be treated is transferred to the evaporator (3D) by the heat pump (3).
There is no wastage of cooling energy because it is used to cool the liquid to be processed and supplied to the cooling section (2A).
以下に本発明の別実施例を示す。 Another example of the present invention will be shown below.
［１］上記実施例では、戻り路（４）を設けたが、本発
明は、戻り路（４〉を設けずに実施しても良い。この場
合、排液等の液濃縮にも適用できるが、純水製造に適用
することが好ましい。[1] In the above embodiment, the return path (4) was provided, but the present invention may be implemented without providing the return path (4). In this case, it can also be applied to liquid concentration such as waste liquid. However, it is preferable to apply it to pure water production.
［２］上記実施例では、液室（１ａ）に供給する被処理
液を加熱することで液室（１ａ）を加熱し、冷却部（２
Ａ）に供給する被処理液を冷却することで気室（１ｂ）
を冷却するようにしたが、第２図に示すように液室（１
ａ）内に凝縮器（３Ｂ）を設置し、気室（１ｂ）又は冷
却室（ｌｃ） ［図面は気室（１ｂ）内に設けて冷却室
（Ｃ）を省いたものを示す。〕内に蒸発器（３Ｄ）を設
置して、液室（１ａ）の加熱、気室（１ｂ）の冷却を行
ってもよい。[2] In the above embodiment, the liquid chamber (1a) is heated by heating the liquid to be treated that is supplied to the liquid chamber (1a), and the cooling section (2a) is heated.
By cooling the liquid to be treated to be supplied to A), the air chamber (1b)
However, as shown in Figure 2, the liquid chamber (1
a) A condenser (3B) is installed inside the air chamber (1b) or a cooling chamber (lc) [The drawing shows the air chamber (1b) installed and the cooling chamber (C) omitted. ] An evaporator (3D) may be installed inside to heat the liquid chamber (1a) and cool the air chamber (1b).
［３］尚、特許請求の範囲の項に図面との対照を便利に
する為に符号を記すが、該記入により本発明は添付図面
の構造に限定されるものではない。[3] Note that although reference numerals are written in the claims section for convenience of comparison with the drawings, the present invention is not limited to the structure shown in the accompanying drawings.
第１図は本発明の実施例を示す概略構成図、第２図は本
発明の別実施例を示す概略構成図であり、第３図、第４
図は従来例を示す概略構成図である。
（１ａ）・・・・・・液室、（１ｂ）・・・・・・気室
、（１）・・・・・・分離器、（２）・・・・・・給液
路、（１Ａ）・・・・・・透過膜、（３）・・・・・・
ヒートポンプ、（３Ｂ）・・・・・・凝縮器、（３Ｄ）
・・・・・・蒸発器、（４）・・・・・・戻り路。FIG. 1 is a schematic block diagram showing an embodiment of the present invention, FIG. 2 is a schematic block diagram showing another embodiment of the present invention, and FIGS.
The figure is a schematic configuration diagram showing a conventional example. (1a)...Liquid chamber, (1b)...Air chamber, (1)...Separator, (2)...Liquid supply path, ( 1A)...Permeable membrane, (3)...
Heat pump, (3B)... Condenser, (3D)
...Evaporator, (4) ...Return path.
Claims (1)
分離器（１）を設け、その分離器（１）の前記液室（１
ａ）に被処理液を供給するための給液路（２）と、前記
液室（１ａ）を気室（１ｂ）よりも高温にするための温
度調整手段とを設け、前記分離器（１）の仕切りに、液
室（１ａ）と気室（１ｂ）との温度差に相当する水蒸気
分圧差をもって液室 （１ａ）から気室（１ｂ）に水蒸気のみを選択的に透過
させる透過膜（１Ａ）を設けてある膜分離装置であって
、前記温度調整手段を構成するに、ヒートポンプ（３）
を設け、そのヒートポンプ（３）の凝縮器（３Ｂ）と蒸
発器（３Ｄ）とのうち、凝縮器（３Ｂ）を液室加熱源と
し、かつ、蒸発器（３Ｄ）を気室冷却源として夫々設け
てある膜分離装置。 ２、前記給液路（２）に被処理液を冷却材として前記気
室（１ｂ）を冷却する冷却部（２Ａ）を設け、その給液
路（２）のうち冷却部（２Ａ）よりも上流側の部分に、
被処理液の冷却器として前記蒸発器（３Ｄ）を設け、冷
却部（２Ａ）から前記液室（１ａ）に到る部分に、被処
理液の加熱器として前記凝縮器（３Ｂ）を設けてある請
求項１記載の膜分離装置。 ３、前記分離器（１）の液室（１ａ）から排出される濃
縮液を前記給液路（２）に戻すための戻り路（４）を設
けてある請求項１又は２記載の膜分離装置。[Claims] 1. A separator (1) whose interior is partitioned into a liquid chamber (1a) and an air chamber (1b) is provided, and the liquid chamber (1) of the separator (1) is
a) is provided with a liquid supply path (2) for supplying the liquid to be treated, and a temperature adjustment means for making the liquid chamber (1a) higher in temperature than the air chamber (1b), and the separator (1 ), a permeable membrane ( 1A), in which the temperature adjusting means comprises a heat pump (3).
Of the condenser (3B) and evaporator (3D) of the heat pump (3), the condenser (3B) serves as a liquid chamber heating source, and the evaporator (3D) serves as an air chamber cooling source, respectively. Membrane separation equipment installed. 2. A cooling part (2A) for cooling the air chamber (1b) using the liquid to be treated as a coolant is provided in the liquid supply path (2), and a cooling part (2A) is provided in the liquid supply path (2). In the upstream part,
The evaporator (3D) is provided as a cooler for the liquid to be treated, and the condenser (3B) is provided as a heater for the liquid to be treated from the cooling section (2A) to the liquid chamber (1a). The membrane separation device according to claim 1. 3. The membrane separation according to claim 1 or 2, further comprising a return path (4) for returning the concentrated liquid discharged from the liquid chamber (1a) of the separator (1) to the liquid supply path (2). Device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21936889A JPH0380920A (en) | 1989-08-25 | 1989-08-25 | Membrane separation apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21936889A JPH0380920A (en) | 1989-08-25 | 1989-08-25 | Membrane separation apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0380920A true JPH0380920A (en) | 1991-04-05 |
Family
ID=16734322
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP21936889A Pending JPH0380920A (en) | 1989-08-25 | 1989-08-25 | Membrane separation apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0380920A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03181302A (en) * | 1989-12-12 | 1991-08-07 | Hitachi Ltd | Distilling apparatus |
| WO2000072947A1 (en) * | 1999-05-27 | 2000-12-07 | Nederlandse Organisatie Voor Toegepast-Natuurwetenschappelijk Onderzoek Tno | Method for the purification of a liquid by membrane distillation, in particular for the production of desalinated water from seawater or brackish water or process water |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4945461A (en) * | 1972-09-06 | 1974-04-30 |
-
1989
- 1989-08-25 JP JP21936889A patent/JPH0380920A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4945461A (en) * | 1972-09-06 | 1974-04-30 |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03181302A (en) * | 1989-12-12 | 1991-08-07 | Hitachi Ltd | Distilling apparatus |
| WO2000072947A1 (en) * | 1999-05-27 | 2000-12-07 | Nederlandse Organisatie Voor Toegepast-Natuurwetenschappelijk Onderzoek Tno | Method for the purification of a liquid by membrane distillation, in particular for the production of desalinated water from seawater or brackish water or process water |
| US6716355B1 (en) | 1999-05-27 | 2004-04-06 | Nederlands Organisatie Voor Toegepast-Natuurwetenshappelijk Onderzoek Tno | Method for the purification of a liquid by membrane distillation, in particular for the production of desalinated water from seawater or brackish water or process water |
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