WO2022030044A1 - Membrane distillation device and method for operating same - Google Patents
Membrane distillation device and method for operating same Download PDFInfo
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- WO2022030044A1 WO2022030044A1 PCT/JP2021/011887 JP2021011887W WO2022030044A1 WO 2022030044 A1 WO2022030044 A1 WO 2022030044A1 JP 2021011887 W JP2021011887 W JP 2021011887W WO 2022030044 A1 WO2022030044 A1 WO 2022030044A1
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- water supply
- pipe
- secondary side
- membrane
- distillation apparatus
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- 239000012528 membrane Substances 0.000 title claims abstract description 58
- 238000004821 distillation Methods 0.000 title claims description 26
- 238000000034 method Methods 0.000 title claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000007788 liquid Substances 0.000 claims abstract description 22
- 238000004891 communication Methods 0.000 claims description 8
- 230000006837 decompression Effects 0.000 claims description 7
- 230000002209 hydrophobic effect Effects 0.000 claims description 6
- 239000012510 hollow fiber Substances 0.000 abstract description 23
- 239000000463 material Substances 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 5
- -1 polyethylene Polymers 0.000 description 5
- 238000004382 potting Methods 0.000 description 5
- 238000009835 boiling Methods 0.000 description 4
- 239000007864 aqueous solution Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000011017 operating method Methods 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 2
- 239000004810 polytetrafluoroethylene Substances 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 239000002033 PVDF binder Substances 0.000 description 1
- 239000004695 Polyether sulfone Substances 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 239000003929 acidic solution Substances 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000007747 plating Methods 0.000 description 1
- 229920002492 poly(sulfone) Polymers 0.000 description 1
- 229920006393 polyether sulfone Polymers 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/362—Pervaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
Definitions
- the present invention relates to a membrane distillation apparatus and an operating method thereof.
- the membrane distillation apparatus passes a heated liquid to be treated to the primary side of a hydrophobic flat membrane or a hydrophobic hollow fiber membrane, and makes the secondary side of the membrane lower than the vapor pressure of the primary side to be treated. It is configured to recover only vapor from the liquid and concentrate the liquid to be treated. Unlike a general distillation apparatus, the membrane distillation apparatus has an advantage that the evaporated surface area is increased and the apparatus is miniaturized by using the membrane.
- FIG. 2 shows an example of a conventional example of a membrane distillation apparatus.
- the liquid to be treated stored in the water supply tank 1 is sent to the heat exchanger (heater) 4 via the pipe 3 having the water supply pump 2, and after heat exchange with the high temperature fluid to be heated, the pipe is used. Water is sent to the membrane module 10 via 5.
- the membrane module 10 is a hollow fiber membrane module.
- a large number of hollow fibers 11 are aligned to form a hollow fiber bundle, which is arranged in the vertical direction.
- the upper end side and the lower end side of the hollow fiber bundle are bound by the potting materials 12 and 13.
- the hollow fiber bundle is arranged in the casing 14 of the membrane module 10, the inflow chamber 15 is formed on the upper side of the upper potting material 12, and the outflow chamber 16 is formed on the lower side of the lower potting material 13.
- the inside of each hollow fiber 11 communicates with the inflow chamber 15 and the outflow chamber 16, respectively.
- the liquid to be treated from the pipe 5 flows from the inflow chamber 15 into each hollow fiber 11 (primary side), passes through the hollow fiber 11, flows to the outflow chamber 16, and flows from the outflow chamber 16 to the water supply tank via the pipe 6. Return to 1.
- the secondary side 17 is outside the hollow fiber 11 in the casing 14 and between the potting materials 12 and 13.
- the secondary side 17 communicates with the decompression device 25 via a pipe (steam pipe) 20, a heat exchanger (cooler) 21, a pipe 22, a condensed water tank 23, and a pipe 24, and the decompression device 25 communicates with the decompression device 25.
- the secondary side 17 is depressurized.
- the water in the liquid to be treated permeates the hollow yarn 11 and becomes vapor, which is sucked and discharged from the secondary side 17 to the pipe 20 and discharged to the pipe 20 to be discharged from the secondary side 17 to the heat exchanger 21. Cooled with to produce condensed water.
- the condensed water is stored in the condensed water tank 23.
- Pressure sensors P1, P2, and P3 are installed so as to detect the pressure in the gas phase portion 1a, the pipe 20, and the pipe 5 of the water supply tank 1.
- the negative pressure of the decompression apparatus 25 is transmitted from the secondary side 17 to the water supply tank 1 via the pipe 7. Therefore, the pressure in the pipe 3 on the suction side of the water supply pump 2 becomes low, and cavitation may occur. In order to prevent this cavitation, it is necessary to increase the head (water surface height) H in the water supply tank 1, and it is necessary to design to increase the height of the water supply tank 1.
- An object of the present invention is to provide a membrane distillation apparatus capable of preventing cavitation of a water supply pump and an operation method thereof without increasing the height of the water supply tank.
- the membrane distillation apparatus of the present invention has a membrane module whose casing is separated into a primary side and a secondary side by a hydrophobic membrane, and a water supply tank for circulating and supplying a liquid to be treated to the primary side of the membrane module.
- a liquid circulation supply means for processing liquid having a water supply pump, a decompression device for reducing the pressure on the secondary side of the membrane module, and a communication means for communicating the secondary side of the membrane module with the gas phase portion of the water supply tank.
- the membrane distillation apparatus is characterized in that the pressure difference between the gas phase portion of the water supply tank and the secondary side of the membrane module is 20 to 90 kPa.
- the communication portion has a pressure difference adjusting means for adjusting the pressure difference.
- the communication portion having the pressure difference adjusting means is a pipe provided with a valve.
- the communication portion is a pipe
- the inner diameter of the pipe is one of the inner diameter of the steam pipe connected to the secondary side so as to depressurize the secondary side and suck and discharge steam. It is less than / 4.
- the operating method of the membrane distillation apparatus of the present invention is the operating method of the membrane distillation apparatus of the present invention, characterized in that the opening degree of the valve is adjusted so that the pressure difference is 20 to 90 kPa.
- the pressure on the suction side of the water supply pump can be secured and cavitation can be prevented.
- FIG. 1 shows the configuration of the membrane distillation apparatus according to the embodiment.
- the pressure difference between the secondary side 17 and the gas phase portion 1a is adjusted in the pipe 7 that communicates the secondary side 17 of the membrane module 10 and the gas phase portion 1a of the water supply tank 1.
- a valve 8 is provided. Instead of providing the valve 8, the diameter of the pipe 7 may be reduced to adjust the pressure difference between the secondary side 17 and the gas phase portion 1a, the diameter of the pipe 7 may be reduced, and the valve may be reduced. 8 may be provided. Further, the diameter of a part of the pipe 7 may be reduced.
- the inner diameter of the pipe 7 is 1/4 (25%) or less of the inner diameter of the steam pipe 20, preferably 0.5 to 25%, and particularly preferably 1 to 20%.
- the pipe 7 is installed for the purpose of discharging the condensate or precipitate accumulated on the secondary side of the membrane module 10 before restarting after the operation of the membrane distillation apparatus is stopped or during the operation, and the inner diameter of the pipe 7 is Even if it is small, there is almost no effect on the operation management of the membrane distillation apparatus.
- the valve 8 is frequently opened and closed in order to stably adjust the pressure difference to a predetermined value, which makes operation management difficult.
- the length of the pipe 7 is preferably 0.2 to 4 m, particularly preferably 0.5 to 2 m.
- the opening degree of the valve 8 (or the pipe diameter of the pipe 7) is set so that 2 is 20 to 90 kPa, preferably 20 to 70 kPa.
- the gauge pressure (difference from atmospheric pressure) of P 2 is preferably about -100 to -40 kPa, particularly preferably about -100 to -60 kPa.
- FIG. 1 The other configurations of FIG. 1 are the same as those of FIG. 2, and the same reference numerals indicate the same parts.
- the inner diameter (diameter) of the hollow yarn is preferably 0.1 to 3.0 mm, particularly 0.5 to 2.0 mm, and the thickness, that is, the difference between the outer diameter (radius) and the inner diameter (radius) of the hollow yarn is 0. 01 to 1.0 mm, particularly 0.1 to 0.5 mm is preferable.
- the length of the hollow fiber is preferably 200 to 2000 mm, particularly preferably 300 to 1000 mm.
- the filling rate of the hollow fibers (sum of the cross-sectional areas of the hollow fibers / the cross-sectional area of the casing) is preferably 5% to 50%, particularly preferably 15% to 35%.
- the material of the hollow fiber include, but are not limited to, polysulfone, polyethersulfone, polyethylene, polypropylene, polyvinylidene fluoride, and polytetrafluoroethylene.
- a hollow fiber is used, but a hydrophobic flat membrane may be used.
- an acidic solution such as salt, phosphoric acid, hydrochloric acid, fluoroacid, sulfuric acid, an alkaline waste liquid such as ammonia water, and an aqueous solution such as plating waste water are suitable.
- the water flow rate (linear velocity) of the liquid to be treated in the hollow fiber is preferably 400 to 2000 mm / sec, particularly about 700 to 1500 mm / sec.
- the temperature of the liquid to be treated when flowing into the membrane module 10 is preferably 45 to 150 ° C., particularly preferably about 50 to 80 ° C.
- Hollow fiber 11 Made of polytetrafluoroethylene, Inner diameter 1.0 mm, thickness 0.3 mm, length 600 mm, casing of single film module 10: inner diameter 10 mm, height 690 mm Water supply: 1% NaCl aqueous solution Water supply temperature: 60 ° C Membrane module inlet pressure P 3 : -80 kPa (gauge pressure) Water supply amount: 40 mL / min (Line speed in hollow fiber 850 mm / sec) Secondary pressure P 2 : -90 kPa (gauge pressure) Inner diameter of steam pipe 20: 6 mm Inner diameter of pipe 7: 6 mm Length of pipe 7: 1m Liquid level H: 50 cm
- FIG. 3 shows the relationship between the pressure and boiling point of this aqueous solution. From this relationship, it is considered that boiling occurs at -80 kPa when the water supply temperature is 60 ° C.
- Example 1 ⁇ Experimental equipment and conditions> The membrane distillation apparatus shown in FIG. 1 having the same configuration as that of Comparative Example 1 was used except that the pipe 7 had an inner diameter of 0.75 mm and the pipe 7 was provided with a valve 8 having an adjustable opening degree (the inner diameter of the pipe 7 is 12.5% of the inner diameter of the steam pipe 20). The distillation test was carried out under the same conditions as in Comparative Example 1 except that the opening degree of the valve 8 was adjusted so that the membrane module inlet pressure P 3 became ⁇ 40 kPa (gauge pressure).
- Example 1 since the inner diameter of the pipe 7 is sufficiently smaller than that of Comparative Example 1, the speed at which the inside of the water supply tank 1 is depressurized is smaller than that of the secondary side 17, and the pressure adjustment is easy.
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- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
In the present invention, a liquid to be treated in a water supply tank 1 is supplied to hollow fibers 11 of a membrane module 10 via a water supply pump 2, a pipe 3, a heat exchanger 4, and a pipe 5, and returns to the water supply tank 1. The pressure of a secondary side 17 is reduced by a pressure reduction device 25. The water of the liquid to be treated which is flowing through the hollow fibers 11 evaporates, and is suctioned and discharged from the secondary side 17 to a pipe 20. A water supply tank gas phase part 1a and the secondary side 17 communicate with each other via a pipe 7 and a valve 8, and the pressure difference p1 - p2 between the water supply tank gas phase part 1a and the secondary side 17 is 20-90 kPa.
Description
本発明は、膜蒸留装置及びその運転方法に関する。
The present invention relates to a membrane distillation apparatus and an operating method thereof.
膜蒸留装置は、疎水性平膜または疎水性中空糸膜の一次側に加温された被処理液を通水し、膜の二次側を一次側の蒸気圧以下にすることで、被処理液から蒸気のみを回収し、被処理液を濃縮するよう構成されている。膜蒸留装置は、一般的な蒸留装置と異なり、膜を用いることによって蒸発表面積が増え、装置が小型化するというメリットを有する。
The membrane distillation apparatus passes a heated liquid to be treated to the primary side of a hydrophobic flat membrane or a hydrophobic hollow fiber membrane, and makes the secondary side of the membrane lower than the vapor pressure of the primary side to be treated. It is configured to recover only vapor from the liquid and concentrate the liquid to be treated. Unlike a general distillation apparatus, the membrane distillation apparatus has an advantage that the evaporated surface area is increased and the apparatus is miniaturized by using the membrane.
膜蒸留装置の従来例の一例を図２に示す。給水タンク１内に貯留された被処理液が給水ポンプ２を有した配管３を介して熱交換器（加温器）４に送水され、高温流体と熱交換して加温された後、配管５を介して膜モジュール１０に送水される。
FIG. 2 shows an example of a conventional example of a membrane distillation apparatus. The liquid to be treated stored in the water supply tank 1 is sent to the heat exchanger (heater) 4 via the pipe 3 having the water supply pump 2, and after heat exchange with the high temperature fluid to be heated, the pipe is used. Water is sent to the membrane module 10 via 5.
この従来例では、膜モジュール１０は中空糸膜モジュールである。膜モジュール１０では、多数本の中空糸１１が引き揃えられて中空糸束とされ、上下方向に配設されている。中空糸束の上端側及び下端側がポッティング材１２，１３で結束されている。
In this conventional example, the membrane module 10 is a hollow fiber membrane module. In the membrane module 10, a large number of hollow fibers 11 are aligned to form a hollow fiber bundle, which is arranged in the vertical direction. The upper end side and the lower end side of the hollow fiber bundle are bound by the potting materials 12 and 13.
中空糸束は膜モジュール１０のケーシング１４内に配置されており、上側ポッティング材１２の上側に流入室１５が形成され、下側ポッティング材１３の下側に流出室１６が形成されている。各中空糸１１内はそれぞれ流入室１５及び流出室１６内に連通している。
The hollow fiber bundle is arranged in the casing 14 of the membrane module 10, the inflow chamber 15 is formed on the upper side of the upper potting material 12, and the outflow chamber 16 is formed on the lower side of the lower potting material 13. The inside of each hollow fiber 11 communicates with the inflow chamber 15 and the outflow chamber 16, respectively.
配管５からの被処理液は、流入室１５から各中空糸１１内（一次側）に流入し、中空糸１１を通り、流出室１６へ流れ、該流出室１６から配管６を介して給水タンク１に戻る。
The liquid to be treated from the pipe 5 flows from the inflow chamber 15 into each hollow fiber 11 (primary side), passes through the hollow fiber 11, flows to the outflow chamber 16, and flows from the outflow chamber 16 to the water supply tank via the pipe 6. Return to 1.
ケーシング１４内における中空糸１１外であって且つポッティング材１２，１３間が二次側１７である。
The secondary side 17 is outside the hollow fiber 11 in the casing 14 and between the potting materials 12 and 13.
該二次側１７は、配管（蒸気配管）２０、熱交換器（冷却器）２１、配管２２、凝縮水タンク２３及び配管２４を介して減圧装置２５に連通しており、該減圧装置２５によって該二次側１７が減圧される。
The secondary side 17 communicates with the decompression device 25 via a pipe (steam pipe) 20, a heat exchanger (cooler) 21, a pipe 22, a condensed water tank 23, and a pipe 24, and the decompression device 25 communicates with the decompression device 25. The secondary side 17 is depressurized.
被処理液が中空糸１７内（一次側）を流れる間に被処理液中の水が中空糸１１を透過し、蒸気となって二次側１７から配管２０へ吸引排出され、熱交換器２１で冷却されて凝縮水が生成する。凝縮水は、凝縮水タンク２３に貯留される。
While the liquid to be treated flows through the hollow yarn 17 (primary side), the water in the liquid to be treated permeates the hollow yarn 11 and becomes vapor, which is sucked and discharged from the secondary side 17 to the pipe 20 and discharged to the pipe 20 to be discharged from the secondary side 17 to the heat exchanger 21. Cooled with to produce condensed water. The condensed water is stored in the condensed water tank 23.
この従来例では、ケーシング１４内の二次側１７と給水タンク１内の上部（気相部１ａ）とが配管７で連通されている。
In this conventional example, the secondary side 17 in the casing 14 and the upper part (gas phase portion 1a) in the water supply tank 1 are communicated with each other by a pipe 7.
給水タンク１の気相部１ａ、配管２０及び配管５内の圧力を検出するように圧力センサＰ１，Ｐ２，Ｐ３が設置されている。
Pressure sensors P1, P2, and P3 are installed so as to detect the pressure in the gas phase portion 1a, the pipe 20, and the pipe 5 of the water supply tank 1.
上記膜蒸留装置にあっては、減圧装置２５の負圧が二次側１７から配管７を介して給水タンク１内に伝達される。そのため、給水ポンプ２の吸込側における配管３内の圧力が低くなり、キャビテーションが発生するおそれがある。このキャビテーションを防止するためには、給水タンク１内の水頭（水面高さ）Ｈを大きくする必要があり、給水タンク１の高さを大きくする設計が必要となる。
In the membrane distillation apparatus, the negative pressure of the decompression apparatus 25 is transmitted from the secondary side 17 to the water supply tank 1 via the pipe 7. Therefore, the pressure in the pipe 3 on the suction side of the water supply pump 2 becomes low, and cavitation may occur. In order to prevent this cavitation, it is necessary to increase the head (water surface height) H in the water supply tank 1, and it is necessary to design to increase the height of the water supply tank 1.
本発明は、給水タンクの高さを大きくすることなく、給水ポンプのキャビテーションを防止することができる膜蒸留装置及びその運転方法を提供することを目的とする。
An object of the present invention is to provide a membrane distillation apparatus capable of preventing cavitation of a water supply pump and an operation method thereof without increasing the height of the water supply tank.
本発明の膜蒸留装置は、ケーシング内が疎水性膜によって一次側と二次側とに隔てられている膜モジュールと、該膜モジュールの一次側に被処理液を循環供給するための、給水タンク及び給水ポンプを有した被処理液循環供給手段と、該膜モジュールの二次側を減圧する減圧装置と、該膜モジュールの二次側と前記給水タンクの気相部とを連通する連通手段とを有する膜蒸留装置において、該給水タンクの気相部と膜モジュールの二次側との圧力差が２０～９０ｋＰａであることを特徴とする。
The membrane distillation apparatus of the present invention has a membrane module whose casing is separated into a primary side and a secondary side by a hydrophobic membrane, and a water supply tank for circulating and supplying a liquid to be treated to the primary side of the membrane module. A liquid circulation supply means for processing liquid having a water supply pump, a decompression device for reducing the pressure on the secondary side of the membrane module, and a communication means for communicating the secondary side of the membrane module with the gas phase portion of the water supply tank. The membrane distillation apparatus is characterized in that the pressure difference between the gas phase portion of the water supply tank and the secondary side of the membrane module is 20 to 90 kPa.
本発明の一態様では、前記連通部は、前記圧力差を調整する圧力差調整手段を有する。
In one aspect of the present invention, the communication portion has a pressure difference adjusting means for adjusting the pressure difference.
本発明の一態様では、前記圧力差調整手段を有する前記連通部は、弁を備えた配管である。
In one aspect of the present invention, the communication portion having the pressure difference adjusting means is a pipe provided with a valve.
本発明の一態様では、前記連通部は配管であり、該配管の内径が、前記二次側を減圧して蒸気を吸引排出するように該二次側に接続された蒸気配管の内径の１／４以下である。
In one aspect of the present invention, the communication portion is a pipe, and the inner diameter of the pipe is one of the inner diameter of the steam pipe connected to the secondary side so as to depressurize the secondary side and suck and discharge steam. It is less than / 4.
本発明の膜蒸留装置の運転方法は、かかる本発明の膜蒸留装置の運転方法であって、前記圧力差が２０～９０ｋＰａとなるように前記弁の開度を調整することを特徴とする。
The operating method of the membrane distillation apparatus of the present invention is the operating method of the membrane distillation apparatus of the present invention, characterized in that the opening degree of the valve is adjusted so that the pressure difference is 20 to 90 kPa.
本発明によると、二次側と給水タンク内の気相部との圧力差を２０～９０ｋＰａに調整することにより、送水ポンプの吸込側の圧力を確保し、キャビテーションを防止することができる。
According to the present invention, by adjusting the pressure difference between the secondary side and the gas phase portion in the water supply tank to 20 to 90 kPa, the pressure on the suction side of the water supply pump can be secured and cavitation can be prevented.
図１は、実施の形態に係る膜蒸留装置の構成を示している。
FIG. 1 shows the configuration of the membrane distillation apparatus according to the embodiment.
この実施の形態では、膜モジュール１０の二次側１７と給水タンク１の気相部１ａとを連通する配管７に、二次側１７と該気相部１ａとの圧力差を調整するための弁８が設けられている。なお、弁８を設ける代りに配管７の径を小さくすることにより、二次側１７と気相部１ａとの圧力差を調整するようにしてもよく、配管７の径を小さくし、且つ弁８を設けるようにしてもよい。また配管７の一部の径を小さくしてもよい。
In this embodiment, the pressure difference between the secondary side 17 and the gas phase portion 1a is adjusted in the pipe 7 that communicates the secondary side 17 of the membrane module 10 and the gas phase portion 1a of the water supply tank 1. A valve 8 is provided. Instead of providing the valve 8, the diameter of the pipe 7 may be reduced to adjust the pressure difference between the secondary side 17 and the gas phase portion 1a, the diameter of the pipe 7 may be reduced, and the valve may be reduced. 8 may be provided. Further, the diameter of a part of the pipe 7 may be reduced.
配管７の径を小さくする場合、配管７の内径は、蒸気配管２０の内径の１／４（２５％）以下、好ましくは０．５～２５％、特に好ましくは１～２０％である。なお配管７は、膜蒸留装置の運転停止後の再起動前または運転中に膜モジュール１０の二次側に滞留する凝縮液又は析出物を排出する目的で設置されており、配管７の内径は小さくても膜蒸留装置の運転管理上の影響はほとんどない。一方、配管７の内径が大きい場合、圧力差を所定値に安定して調整するには弁８の開閉を頻繁に行うことになり運転管理が難しくなる。また弁８を閉にした場合は膜モジュール１０の二次側に凝縮液又は析出物が滞留する可能性があり、膜蒸留装置の安定運転上問題となる。
また配管７の長さは０．２～４ｍ、特に０．５～２ｍであることが好ましい。 When the diameter of thepipe 7 is reduced, the inner diameter of the pipe 7 is 1/4 (25%) or less of the inner diameter of the steam pipe 20, preferably 0.5 to 25%, and particularly preferably 1 to 20%. The pipe 7 is installed for the purpose of discharging the condensate or precipitate accumulated on the secondary side of the membrane module 10 before restarting after the operation of the membrane distillation apparatus is stopped or during the operation, and the inner diameter of the pipe 7 is Even if it is small, there is almost no effect on the operation management of the membrane distillation apparatus. On the other hand, when the inner diameter of the pipe 7 is large, the valve 8 is frequently opened and closed in order to stably adjust the pressure difference to a predetermined value, which makes operation management difficult. Further, when the valve 8 is closed, the condensed liquid or the precipitate may stay on the secondary side of the membrane module 10, which causes a problem in stable operation of the membrane distillation apparatus.
The length of thepipe 7 is preferably 0.2 to 4 m, particularly preferably 0.5 to 2 m.
また配管７の長さは０．２～４ｍ、特に０．５～２ｍであることが好ましい。 When the diameter of the
The length of the
本発明では、圧力センサＰ１で検出される給水タンクの気相部１ａの圧力Ｐ１と、圧力センサＰ２によって検出されるケーシング１４内の二次側１７の圧力Ｐ２との差Ｐ１－Ｐ２が２０～９０ｋＰａ好ましくは２０～７０ｋＰａとなるように弁８の開度（又は配管７の管径）を設定する。
In the present invention, the difference P1 −P between the pressure P1 of the gas phase portion 1a of the water supply tank detected by the pressure sensor P1 and the pressure P2 of the secondary side 17 in the casing 14 detected by the pressure sensor P2. The opening degree of the valve 8 (or the pipe diameter of the pipe 7) is set so that 2 is 20 to 90 kPa, preferably 20 to 70 kPa.
これにより、気相部１ａの過度な圧力低下が防止され、給水タンク１の水頭Ｈを大きくすることなく、給水ポンプ２の吸込側でのキャビテーションを防止することができる。
As a result, an excessive pressure drop in the gas phase portion 1a can be prevented, and cavitation on the suction side of the water supply pump 2 can be prevented without increasing the head H of the water supply tank 1.
Ｐ２のゲージ圧（大気圧との差）は－１００～－４０ｋＰａ特に－１００～－６０ｋＰａ程度が好ましい。
The gauge pressure (difference from atmospheric pressure) of P 2 is preferably about -100 to -40 kPa, particularly preferably about -100 to -60 kPa.
なお、図１のその他の構成は図２と同様であり、同一符号は同一部分を示している。
The other configurations of FIG. 1 are the same as those of FIG. 2, and the same reference numerals indicate the same parts.
上記中空糸１１としては、疎水性中空糸膜が好適である。中空糸の内径（直径）は０．１～３．０ｍｍ特に０．５～２．０ｍｍであることが好ましく、厚みすなわち中空糸の外径（半径）と内径（半径）との差は０．０１～１．０ｍｍ、特に０．１～０．５ｍｍが好ましい。中空糸の長さは２００～２０００ｍｍ、特に３００～１０００ｍｍが好ましい。中空糸の充填率(中空糸の断面積の和/ケーシングの断面積)は５％～５０％、特に１５％～３５％が好ましい。中空糸の素材としては、ポリスルホン、ポリエーテルスルホン、ポリエチレン、ポリプロピレン、ポリフッ化ビニリデン及びポリテトラフルオロエチレンなどが例示されるが、これらに限定されない。
As the hollow fiber 11, a hydrophobic hollow fiber membrane is suitable. The inner diameter (diameter) of the hollow yarn is preferably 0.1 to 3.0 mm, particularly 0.5 to 2.0 mm, and the thickness, that is, the difference between the outer diameter (radius) and the inner diameter (radius) of the hollow yarn is 0. 01 to 1.0 mm, particularly 0.1 to 0.5 mm is preferable. The length of the hollow fiber is preferably 200 to 2000 mm, particularly preferably 300 to 1000 mm. The filling rate of the hollow fibers (sum of the cross-sectional areas of the hollow fibers / the cross-sectional area of the casing) is preferably 5% to 50%, particularly preferably 15% to 35%. Examples of the material of the hollow fiber include, but are not limited to, polysulfone, polyethersulfone, polyethylene, polypropylene, polyvinylidene fluoride, and polytetrafluoroethylene.
上記説明では、中空糸が用いられているが、疎水性平膜が用いられてもよい。
In the above description, a hollow fiber is used, but a hydrophobic flat membrane may be used.
被処理液としては、食塩、リン酸、塩酸、弗酸、硫酸等の酸性溶液、アンモニア水のようなアルカリ廃液、メッキ廃水などの水溶液が好適である。中空糸内における被処理液の通水速度（線速度）は４００～２０００ｍｍ／ｓｅｃ、特に７００～１５００ｍｍ／ｓｅｃ程度が好適である。膜モジュール１０に流入する際の被処理液の温度は４５～１５０℃、特に５０～８０℃程度が好適である。
As the liquid to be treated, an acidic solution such as salt, phosphoric acid, hydrochloric acid, fluoroacid, sulfuric acid, an alkaline waste liquid such as ammonia water, and an aqueous solution such as plating waste water are suitable. The water flow rate (linear velocity) of the liquid to be treated in the hollow fiber is preferably 400 to 2000 mm / sec, particularly about 700 to 1500 mm / sec. The temperature of the liquid to be treated when flowing into the membrane module 10 is preferably 45 to 150 ° C., particularly preferably about 50 to 80 ° C.
なお、上記の好適な条件は、好適な一例を示すものであり、本発明は上記条件に限定されるものではない。
The above-mentioned suitable conditions show a suitable example, and the present invention is not limited to the above-mentioned conditions.
［比較例１］
＜実験装置および条件＞
図２に示す装置を下記条件で運転したときの給水タンク内圧力Ｐ１と、膜二次側の圧力Ｐ２の値を測定した。試験条件は以下のとおりである。 [Comparative Example 1]
<Experimental equipment and conditions>
The values of the pressure P1 in the water supply tank and the pressure P2 on the secondary side of the membrane when the apparatus shown in FIG. 2 was operated under the following conditions were measured. The test conditions are as follows.
＜実験装置および条件＞
図２に示す装置を下記条件で運転したときの給水タンク内圧力Ｐ１と、膜二次側の圧力Ｐ２の値を測定した。試験条件は以下のとおりである。 [Comparative Example 1]
<Experimental equipment and conditions>
The values of the pressure P1 in the water supply tank and the pressure P2 on the secondary side of the membrane when the apparatus shown in FIG. 2 was operated under the following conditions were measured. The test conditions are as follows.
中空糸１１：ポリテトラフルオロエチレン製、
内径１．０ｍｍ、厚さ０．３ｍｍ、長さ６００ｍｍ、１本
膜モジュール１０のケーシング１４：内径１０ｍｍ、高さ６９０ｍｍ
給水：ＮａＣｌ １％水溶液
給水温度：６０℃
膜モジュール入口圧力Ｐ３：－８０ｋＰａ（ゲージ圧）
給水量：４０ｍＬ／ｍｉｎ（中空糸内の線速度８５０ｍｍ／ｓｅｃ）
二次側圧力Ｐ２：－９０ｋＰａ（ゲージ圧）
蒸気配管２０の内径：６ｍｍ
配管７の内径：６ｍｍ
配管７の長さ：１ｍ
液面高さＨ：５０ｃｍ Hollow fiber 11: Made of polytetrafluoroethylene,
Inner diameter 1.0 mm, thickness 0.3 mm, length 600 mm, casing of single film module 10:inner diameter 10 mm, height 690 mm
Water supply: 1% NaCl aqueous solution Water supply temperature: 60 ° C
Membrane module inlet pressure P 3 : -80 kPa (gauge pressure)
Water supply amount: 40 mL / min (Line speed in hollow fiber 850 mm / sec)
Secondary pressure P 2 : -90 kPa (gauge pressure)
Inner diameter of steam pipe 20: 6 mm
Inner diameter of pipe 7: 6 mm
Length of pipe 7: 1m
Liquid level H: 50 cm
内径１．０ｍｍ、厚さ０．３ｍｍ、長さ６００ｍｍ、１本
膜モジュール１０のケーシング１４：内径１０ｍｍ、高さ６９０ｍｍ
給水：ＮａＣｌ １％水溶液
給水温度：６０℃
膜モジュール入口圧力Ｐ３：－８０ｋＰａ（ゲージ圧）
給水量：４０ｍＬ／ｍｉｎ（中空糸内の線速度８５０ｍｍ／ｓｅｃ）
二次側圧力Ｐ２：－９０ｋＰａ（ゲージ圧）
蒸気配管２０の内径：６ｍｍ
配管７の内径：６ｍｍ
配管７の長さ：１ｍ
液面高さＨ：５０ｃｍ Hollow fiber 11: Made of polytetrafluoroethylene,
Inner diameter 1.0 mm, thickness 0.3 mm, length 600 mm, casing of single film module 10:
Water supply: 1% NaCl aqueous solution Water supply temperature: 60 ° C
Membrane module inlet pressure P 3 : -80 kPa (gauge pressure)
Water supply amount: 40 mL / min (Line speed in hollow fiber 850 mm / sec)
Secondary pressure P 2 : -90 kPa (gauge pressure)
Inner diameter of steam pipe 20: 6 mm
Inner diameter of pipe 7: 6 mm
Length of pipe 7: 1m
Liquid level H: 50 cm
＜結果、考察＞
膜二次側が減圧されると同時に、給水タンク１内の圧力も急激に減少し、給水タンク圧力Ｐ１が－７０ｋＰａに達した段階で、キャビテーションが生じ、－８０ｋＰａに達した段階で沸騰が始まった。 <Results, consideration>
At the same time as the pressure on the secondary side of the membrane is reduced, the pressure inside thewater supply tank 1 also decreases sharply, cavitation occurs when the water supply tank pressure P 1 reaches -70 kPa, and boiling begins when it reaches -80 kPa. rice field.
膜二次側が減圧されると同時に、給水タンク１内の圧力も急激に減少し、給水タンク圧力Ｐ１が－７０ｋＰａに達した段階で、キャビテーションが生じ、－８０ｋＰａに達した段階で沸騰が始まった。 <Results, consideration>
At the same time as the pressure on the secondary side of the membrane is reduced, the pressure inside the
図３にこの水溶液の圧力と沸点との関係を示す。この関係より、給水温度が６０℃であれば－８０ｋＰａで沸騰が生じると考えられる。
FIG. 3 shows the relationship between the pressure and boiling point of this aqueous solution. From this relationship, it is considered that boiling occurs at -80 kPa when the water supply temperature is 60 ° C.
この比較例１は、－７０ｋＰａの段階でキャビテーションが生じたため、－９０ｋＰａに達した段階でもキャビテーションが生じないようにするためには少なくとも３ｍ相当の液面高さが必要であると考えられる。
In this Comparative Example 1, since cavitation occurred at the stage of -70 kPa, it is considered that a liquid level height equivalent to at least 3 m is required to prevent cavitation even at the stage of reaching -90 kPa.
［実施例１］
＜実験装置および条件＞
配管７を内径０．７５ｍｍのものとし、配管７に開度調整可能な弁８を設けたこと以外は比較例１と同一構成の図１に示す膜蒸留装置を用いた（配管７の内径は蒸気配管２０の内径の１２．５％）。膜モジュール入口圧力Ｐ３が－４０ｋＰａ（ゲージ圧）となるように弁８の開度を調整したこと以外は比較例１と同一条件にて蒸留試験を行った。 [Example 1]
<Experimental equipment and conditions>
The membrane distillation apparatus shown in FIG. 1 having the same configuration as that of Comparative Example 1 was used except that thepipe 7 had an inner diameter of 0.75 mm and the pipe 7 was provided with a valve 8 having an adjustable opening degree (the inner diameter of the pipe 7 is 12.5% of the inner diameter of the steam pipe 20). The distillation test was carried out under the same conditions as in Comparative Example 1 except that the opening degree of the valve 8 was adjusted so that the membrane module inlet pressure P 3 became −40 kPa (gauge pressure).
＜実験装置および条件＞
配管７を内径０．７５ｍｍのものとし、配管７に開度調整可能な弁８を設けたこと以外は比較例１と同一構成の図１に示す膜蒸留装置を用いた（配管７の内径は蒸気配管２０の内径の１２．５％）。膜モジュール入口圧力Ｐ３が－４０ｋＰａ（ゲージ圧）となるように弁８の開度を調整したこと以外は比較例１と同一条件にて蒸留試験を行った。 [Example 1]
<Experimental equipment and conditions>
The membrane distillation apparatus shown in FIG. 1 having the same configuration as that of Comparative Example 1 was used except that the
＜結果、考察＞
本実施例では、膜モジュール入口圧力Ｐ３が－４０ｋＰａとなるように弁８の開度を調整しているため、Ｐ１－Ｐ２が５０ｋＰａとなり、ポンプ２がキャビテーションすることなく運転することが可能であった。 <Results, consideration>
In this embodiment, since the opening degree of thevalve 8 is adjusted so that the membrane module inlet pressure P 3 becomes −40 kPa, P 1 − P 2 becomes 50 kPa, and the pump 2 can be operated without cavitation. It was possible.
本実施例では、膜モジュール入口圧力Ｐ３が－４０ｋＰａとなるように弁８の開度を調整しているため、Ｐ１－Ｐ２が５０ｋＰａとなり、ポンプ２がキャビテーションすることなく運転することが可能であった。 <Results, consideration>
In this embodiment, since the opening degree of the
また、実施例１では配管７の内径が比較例１と比較して十分に小さいため、給水タンク１内が減圧される速度が二次側１７に比べて小さく、圧力調整が容易であった。
Further, in Example 1, since the inner diameter of the pipe 7 is sufficiently smaller than that of Comparative Example 1, the speed at which the inside of the water supply tank 1 is depressurized is smaller than that of the secondary side 17, and the pressure adjustment is easy.
以上より、給水タンク圧力を２０～９０ｋＰａに調整することで、５０ｃｍの液面高さでも、キャビテーションを起こさずに運転が可能であることが確認された。
From the above, it was confirmed that by adjusting the water supply tank pressure to 20 to 90 kPa, it is possible to operate without causing cavitation even at a liquid level of 50 cm.
本発明を特定の態様を用いて詳細に説明したが、本発明の意図と範囲を離れることなく様々な変更が可能であることは当業者に明らかである。
本出願は、２０２０年８月７日付で出願された日本特許出願２０２０－１３４７２７に基づいており、その全体が引用により援用される。 Although the present invention has been described in detail using specific embodiments, it will be apparent to those skilled in the art that various modifications can be made without departing from the intent and scope of the invention.
This application is based on Japanese Patent Application No. 2020-134727 filed on August 7, 2020, which is incorporated by reference in its entirety.
本出願は、２０２０年８月７日付で出願された日本特許出願２０２０－１３４７２７に基づいており、その全体が引用により援用される。 Although the present invention has been described in detail using specific embodiments, it will be apparent to those skilled in the art that various modifications can be made without departing from the intent and scope of the invention.
This application is based on Japanese Patent Application No. 2020-134727 filed on August 7, 2020, which is incorporated by reference in its entirety.
１ 給水タンク
２ 給水ポンプ
４，２１ 熱交換器
８ 弁
１０ 膜モジュール
１１ 中空糸
１２，１３ ポッティング材
１４ ケーシング
１５ 流入室
１６ 流出室
１７ 二次側
２５ 減圧装置 1Water supply tank 2 Water supply pump 4,21 Heat exchanger 8 Valve 10 Membrane module 11 Hollow fiber 12,13 Potting material 14 Casing 15 Inflow chamber 16 Outflow chamber 17 Secondary side 25 Decompression device
２ 給水ポンプ
４，２１ 熱交換器
８ 弁
１０ 膜モジュール
１１ 中空糸
１２，１３ ポッティング材
１４ ケーシング
１５ 流入室
１６ 流出室
１７ 二次側
２５ 減圧装置 1
Claims (5)
- ケーシング内が疎水性膜によって一次側と二次側とに隔てられている膜モジュールと、
該膜モジュールの一次側に被処理液を循環供給するための、給水タンク及び給水ポンプを有した被処理液循環供給手段と、
該膜モジュールの二次側を減圧する減圧装置と、
該膜モジュールの二次側と前記給水タンクの気相部とを連通する連通手段と
を有する膜蒸留装置において、
該給水タンクの気相部と膜モジュールの二次側との圧力差が２０～９０ｋＰａであることを特徴とする膜蒸留装置。 A membrane module whose casing is separated into a primary side and a secondary side by a hydrophobic membrane,
A liquid to be treated circulating supply means having a water supply tank and a water supply pump for circulating and supplying the liquid to be treated to the primary side of the membrane module.
A decompression device that decompresses the secondary side of the membrane module,
In a membrane distillation apparatus having a communication means for communicating the secondary side of the membrane module and the gas phase portion of the water supply tank.
A membrane distillation apparatus characterized in that the pressure difference between the gas phase portion of the water supply tank and the secondary side of the membrane module is 20 to 90 kPa. - 前記連通部は、前記圧力差を調整する圧力差調整手段を有する請求項１の膜蒸留装置。 The membrane distillation apparatus according to claim 1, wherein the communication unit has a pressure difference adjusting means for adjusting the pressure difference.
- 前記圧力差調整手段を有する前記連通部は、弁を備えた配管である請求項２の膜蒸留装置。 The membrane distillation apparatus according to claim 2, wherein the communication portion having the pressure difference adjusting means is a pipe provided with a valve.
- 前記連通部は配管であり、該配管の内径が、前記二次側を減圧して蒸気を吸引排出するように該二次側に接続された蒸気配管の内径の１／４以下である請求項１の膜蒸留装置。 The communication portion is a pipe, and the inner diameter of the pipe is 1/4 or less of the inner diameter of the steam pipe connected to the secondary side so as to depressurize the secondary side and suck and discharge steam. 1 membrane distillation apparatus.
- 請求項３の膜蒸留装置の運転方法であって、前記圧力差が２０～９０ｋＰａとなるように前記弁の開度を調整することを特徴とする膜蒸留装置の運転方法。 The method for operating the membrane distillation apparatus according to claim 3, wherein the opening degree of the valve is adjusted so that the pressure difference is 20 to 90 kPa.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JPH0352627A (en) * | 1989-07-19 | 1991-03-06 | Hitachi Ltd | Membrane distillation apparatus |
| CN1254303C (en) * | 2004-04-27 | 2006-05-03 | 内蒙古工业大学 | Method for increasing flux of membrane distillation and membrane distillation device |
| US20100051549A1 (en) * | 2008-08-29 | 2010-03-04 | Milton Roy Company | Heat recuperating membrane distillation apparatus and system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04346823A (en) * | 1991-05-27 | 1992-12-02 | Hitachi Ltd | Membrane method and device for evaporating and concentrating waste liquid |
| JP2015100776A (en) * | 2013-11-27 | 2015-06-04 | 住友電気工業株式会社 | Wastewater treatment method, membrane distillation module, and wastewater treatment device |
| JP2018083189A (en) * | 2016-05-24 | 2018-05-31 | 旭化成株式会社 | Film distillation apparatus |
| US20170354931A1 (en) * | 2016-06-14 | 2017-12-14 | Korea Institute Of Science And Technology | Membrane distillation system which is capable of real-time monitoring on membrane scaling |
| CN108704484A (en) * | 2018-06-06 | 2018-10-26 | 大连理工大学 | A kind of membrane contactor separation method for polynary pollutant aqueous solution |
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| CN116033959A (en) | 2023-04-28 |
| JP6958687B1 (en) | 2021-11-02 |
| JP2022030607A (en) | 2022-02-18 |
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