CN105683092A - Combined membrane separation process for concentrating IPA from wastewater containing IPA and treating wastewater - Google Patents
Combined membrane separation process for concentrating IPA from wastewater containing IPA and treating wastewater Download PDFInfo
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
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Abstract
Description
技术领域technical field
本发明涉及用于对含有IPA的废水进行IPA的浓缩及废水处理的复合膜分离方法，更具体涉及将渗透蒸发膜分离工序和反渗透膜分离工序结合起来，能够从含有IPA的废水中分离及浓缩IPA并且同时处理废水的复合膜分离方法。The present invention relates to the composite membrane separation method that is used to carry out the concentration of IPA and waste water treatment to the waste water that contains IPA, more specifically relates to the pervaporation membrane separation process and the reverse osmosis membrane separation process to combine, can be separated from the waste water that contains IPA and A composite membrane separation method that concentrates IPA and treats wastewater at the same time.
背景技术Background technique
IPA(异丙醇)在产业车间特别是半导体制造工序及LCD制造工序等中多作为清洗溶液使用，该使用后的清洗废水中通常含有5重量％～15重量％的IPA。关于这样产生的废水，从有机化合物尤其是醇的回收的方面来看，因为IPA的浓度非常低，所以在使用通常的蒸馏工序进行分离、浓缩时没有经济性，因此当前存在对其全部进行废水处理的问题。IPA (isopropanol) is often used as a cleaning solution in industrial workshops, especially in semiconductor manufacturing processes and LCD manufacturing processes, and the cleaning wastewater after use usually contains 5% to 15% by weight of IPA. Regarding the wastewater generated in this way, from the viewpoint of recovery of organic compounds, especially alcohol, since the concentration of IPA is very low, it is not economical to separate and concentrate it using the usual distillation process. deal with the problem.
另一方面，关于这样的IPA清洗废水，从废水处理的方面来看，因为IPA的浓度过高，所以存在用水来稀释，使IPA的浓度降低至1％以下进行废水处理的其它问题。On the other hand, regarding such IPA cleaning wastewater, from the viewpoint of wastewater treatment, since the concentration of IPA is too high, there is another problem of diluting with water to reduce the concentration of IPA to 1% or less for wastewater treatment.
已有关于渗透蒸发膜分离工序的在先研究(专利文献1、2)，该渗透蒸发膜分离工序用于使用渗透蒸发膜从IPA等醇/水的混合溶液中选择性地分离水或者从有机化合物水溶液中选择性地分离有机化合物，而使用反渗透膜分离工序处理废水的技术也广为人知(专利文献3、4)，但渗透蒸发膜分离工序和反渗透膜分离工序是根据用途及特性分别作为不同工序来进行的。There have been previous studies (Patent Documents 1, 2) on pervaporation membrane separation processes for selectively separating water from alcohol/water mixed solutions such as IPA or organic solvents using pervaporation membranes. The technology of selectively separating organic compounds from an aqueous compound solution and using a reverse osmosis membrane separation process to treat wastewater is also known (Patent Documents 3 and 4), but the pervaporation membrane separation process and the reverse osmosis membrane separation process are used as carried out by different processes.
因此，对于不适于进行浓缩来回收再用或进行废水处理的浓度的IPA清洗废水，如果在使用渗透蒸发膜分离工序来浓缩IPA的同时，一并使用反渗透膜分离工序分离IPA而使IPA浓度变成适于废水处理的浓度，则从以往全部要进行废水处理的IPA清洗废水能够选择性地分离及浓缩IPA来回收再用，并且，低浓度的IPA清洗废水能够不进行其它稀释而在已有的废水处理厂直接进行处理，本发明者着眼于上述情况，完成了本发明。Therefore, for the IPA cleaning wastewater that is not suitable for concentration to recycle or carry out wastewater treatment concentration, if using the pervaporation membrane separation process to concentrate IPA, use the reverse osmosis membrane separation process to separate IPA together to make the IPA concentration If it becomes a concentration suitable for wastewater treatment, all the IPA cleaning wastewater that has been treated in the past can be selectively separated and concentrated for recycling, and the low-concentration IPA cleaning wastewater can be used without other dilution. Some waste water treatment plants directly treat the waste water, and the present inventors have completed the present invention focusing on the above-mentioned situation.
现有技术文献prior art literature
专利文献patent documents
专利文献1：日本公开特许公报第10－2011－0083077号；Patent Document 1: Japanese Laid-Open Patent Publication No. 10-2011-0083077;
专利文献2：日本公开特许公报第10－2000－0067454号；Patent Document 2: Japanese Laid-Open Patent Publication No. 10-2000-0067454;
专利文献3：日本公开特许公报第10－2013－0032294号；Patent Document 3: Japanese Laid-Open Patent Publication No. 10-2013-0032294;
专利文献4：日本公开特许公报第10－2005－0026294号。Patent Document 4: Japanese Laid-Open Patent Publication No. 10-2005-0026294.
发明内容Contents of the invention
发明要解决的问题The problem to be solved by the invention
本发明是鉴于上述的问题而做出的，其目的在于提供一种结合了渗透蒸发膜分离工序和反渗透膜分离工序的复合膜分离方法，能够从IPA清洗废水中选择性地分离IPA并将其浓缩至30重量％以上来回收再用，并且0.5重量％以下的低浓度的IPA清洗废水能够不进行其它稀释而在已有的废水处理厂直接进行处理。The present invention is made in view of the above-mentioned problems, and its purpose is to provide a kind of composite membrane separation method that has combined pervaporation membrane separation process and reverse osmosis membrane separation process, can separate IPA selectively from IPA cleaning waste water and It is concentrated to more than 30% by weight for recovery and reuse, and low-concentration IPA cleaning wastewater below 0.5% by weight can be directly treated in existing wastewater treatment plants without other dilution.
用于解决问题的方案solutions to problems
为了实现所述目的，本发明提供一种复合膜分离方法，包括：I)通过渗透蒸发膜分离工序从含有IPA的废水中浓缩IPA的步骤；以及II)通过反渗透膜分离工序从含有IPA的废水处理废水的步骤。In order to achieve said object, the invention provides a kind of composite membrane separation method, comprising: 1) the step of concentrating IPA from the wastewater containing IPA by pervaporation membrane separation process; Wastewater Treatment of wastewater steps.
其特征在于，所述I)步骤的渗透蒸发膜分离工序包括：i)将升温了的含有IPA的废水供给到渗透蒸发膜模块的步骤；ii)将渗透过了渗透蒸发膜模块的IPA凝结为液相的步骤；以及iii)将凝结了的IPA移送到渗透溶液箱的步骤。It is characterized in that, the pervaporation membrane separation process of the step I) includes: i) the step of supplying the heated wastewater containing IPA to the pervaporation membrane module; ii) condensing the IPA permeated through the pervaporation membrane module into the step of the liquid phase; and iii) the step of transferring the coagulated IPA to the permeate solution tank.
其特征在于，所述升温了的含有IPA的废水被加热器维持在30℃～60℃。It is characterized in that the heated wastewater containing IPA is maintained at 30°C to 60°C by a heater.
其特征在于，供给到所述渗透蒸发膜模块的含有IPA的废水的供给流量为渗透流量的5倍以上。It is characterized in that the supply flow rate of the wastewater containing IPA supplied to the pervaporation membrane module is more than 5 times of the permeate flow rate.
其特征在于，所述II)步骤的反渗透膜分离工序包括：a)将升压了的含有IPA的废水供给到反渗透膜模块的步骤；以及b)将渗透过了反渗透膜模块的废水移送到渗透水箱的步骤。It is characterized in that, the reverse osmosis membrane separation process of said II) step includes: a) the step of supplying the boosted wastewater containing IPA to the reverse osmosis membrane module; Step to move to permeate tank.
其特征在于，所述升压了的含有IPA的废水被高压泵维持在10bar～70bar。It is characterized in that the boosted wastewater containing IPA is maintained at 10bar-70bar by a high-pressure pump.
其特征在于，供给到所述反渗透膜模块的含有IPA的废水的供给流量为渗透流量的3倍以上。It is characterized in that the supply flow rate of the wastewater containing IPA supplied to the reverse osmosis membrane module is more than three times the permeate flow rate.
发明效果Invention effect
根据本发明的复合膜分离方法，能够从IPA清洗废水中选择性地分离IPA，将其浓缩至30重量％以上来回收再用，并且同时能够将0.5重量％以下的低浓度的IPA清洗废水不进行其它稀释而在已有的废水处理厂直接进行处理。According to the composite membrane separation method of the present invention, IPA can be selectively separated from the IPA cleaning wastewater, and it can be concentrated to more than 30% by weight for recycling, and at the same time, the low-concentration IPA cleaning wastewater below 0.5% by weight can not be used. Other dilutions are carried out for direct treatment in existing wastewater treatment plants.
附图说明Description of drawings
图1是示出本发明的连续式(continuous)复合膜分离方法的框图；Fig. 1 is the block diagram showing continuous type (continuous) composite membrane separation method of the present invention;
图2是示出本发明的分批式(batch)复合膜分离方法的框图。Fig. 2 is a block diagram showing a batch composite membrane separation method of the present invention.
具体实施方式detailed description
以下，详细说明本发明的使用渗透蒸发膜分离工序浓缩IPA并且同时使用反渗透膜分离工序分离IPA以使IPA浓度适于废水处理的浓度的复合膜分离方法和附图。Hereinafter, the composite membrane separation method of the present invention that uses the pervaporation membrane separation process to concentrate IPA and simultaneously uses the reverse osmosis membrane separation process to separate IPA so that the concentration of IPA is suitable for wastewater treatment and the accompanying drawings will be described in detail.
本发明提供一种复合膜分离方法，包括：I)通过渗透蒸发膜分离工序从含有IPA的废水中浓缩IPA的步骤；以及II)通过反渗透膜分离工序从含有IPA的废水处理废水的步骤。The invention provides a composite membrane separation method, comprising: I) a step of concentrating IPA from wastewater containing IPA through a pervaporation membrane separation process; and II) a step of treating wastewater from the wastewater containing IPA through a reverse osmosis membrane separation process.
此外，上述I)步骤的渗透蒸发膜分离工序包括：i)将升温了的含有IPA的废水供给到渗透蒸发膜模块的步骤；ii)将渗透过了渗透蒸发膜模块的IPA凝结为液相的步骤；以及iii)将凝结了的IPA移送到渗透溶液箱的步骤，如图1的连续(continuous)工序框图所示，首先，将含有IPA的废水(IPA溶液)贮存于IPA溶液箱100，利用加热器110等通常的加热单元使IPA溶液箱的IPA溶液升温。此时，如果IPA溶液的温度不足30℃，则渗透蒸发膜模块的渗透量过小，如果IPA溶液的温度超过60℃，则能量消耗过大，因此，优选IPA溶液通过加热器110升温而维持在30℃～60℃。In addition, the pervaporation membrane separation process of the above-mentioned I) step includes: i) the step of supplying the heated wastewater containing IPA to the pervaporation membrane module; ii) condensing the IPA permeated through the pervaporation membrane module into liquid phase and iii) the step of transferring the coagulated IPA to the permeation solution tank, as shown in the continuous (continuous) process block diagram of Figure 1, at first, the waste water (IPA solution) containing IPA is stored in the IPA solution tank 100, using Common heating means such as the heater 110 raises the temperature of the IPA solution in the IPA solution tank. At this time, if the temperature of the IPA solution is less than 30°C, the permeation amount of the pervaporation membrane module is too small, and if the temperature of the IPA solution exceeds 60°C, the energy consumption is too large. Therefore, it is preferable that the IPA solution is heated by the heater 110 to maintain Between 30°C and 60°C.
接着，将升温至30℃～60℃的IPA溶液供给到渗透蒸发膜模块150，在此，伴随着依次经过IPA溶液供给泵120、溶液过滤器130及IPA溶液流量计140的过程。此时，优选供给到渗透蒸发膜模块150的IPA溶液的供给流量调节为渗透流量的5倍以上。如果将IPA溶液以渗透流量的5倍以下供给到渗透蒸发膜模块150，则通过渗透蒸发膜模块150渗透的渗透溶液的IPA的浓度低，因此，不能顺畅地进行分离及浓缩。Next, the IPA solution heated to 30° C. to 60° C. is supplied to the pervaporation membrane module 150 , where it passes through the IPA solution supply pump 120 , the solution filter 130 and the IPA solution flow meter 140 in sequence. At this time, it is preferable to adjust the supply flow rate of the IPA solution supplied to the pervaporation membrane module 150 to 5 times or more of the permeation flow rate. If the IPA solution is supplied to the pervaporation membrane module 150 at 5 times or less the permeate flow rate, the permeate solution that permeates through the pervaporation membrane module 150 will have a low IPA concentration, and thus cannot be separated and concentrated smoothly.
像这样供给到渗透蒸发膜模块150的IPA溶液具有IPA在分离膜内溶解，在分离膜内扩散而以气相渗透的作用机理。根据这种作用机理，渗透蒸发膜模块150的一端与IPA供给溶液接触，另一端与低的渗透物的蒸汽压接触，低的蒸汽压条件能够通过抽真空或者使惰性载气流入而生成。因此，通常，在渗透蒸发膜的内部产生作为渗透蒸发膜分离工序的推进力(drivingforce)的化学势能的梯度，进行物质经由膜的渗透，因此，在本发明中，为了维持渗透蒸发膜分离工序的推进力，通过使用真空泵170而使渗透部维持真空。The IPA solution supplied to the pervaporation membrane module 150 in this way has an action mechanism in which IPA dissolves in the separation membrane, diffuses in the separation membrane, and permeates in the gas phase. According to this mechanism of action, one end of the pervaporation membrane module 150 is in contact with the IPA feed solution, and the other end is in contact with the low vapor pressure of the permeate, which can be generated by evacuating or flowing an inert carrier gas. Therefore, generally, a gradient of chemical potential energy as a driving force (driving force) of the pervaporation membrane separation process is generated inside the pervaporation membrane, and the permeation of the substance through the membrane is carried out. Therefore, in the present invention, in order to maintain the pervaporation membrane separation process The impulsive force of the vacuum pump 170 is used to maintain a vacuum in the permeate part.
其次，渗透过了渗透蒸发膜模块150的气相的IPA在通常的凝结器160凝结为液相，凝结了的液相的IPA经过渗透溶液流量计180而被移送到渗透溶液箱190。通过该渗透蒸发膜分离工序获得的IPA溶液被浓缩为30％以上，因此能够被回收再用。Next, the gas-phase IPA permeated through the pervaporation membrane module 150 is condensed into a liquid phase in a normal condenser 160 , and the condensed liquid-phase IPA is transferred to the permeate solution tank 190 through the permeate solution flow meter 180 . The IPA solution obtained by this pervaporation membrane separation process is concentrated to 30% or more, so it can be recovered and reused.
另一方面，在本发明的复合膜分离方法中同时进行反渗透膜分离工序，上述II)步骤的反渗透膜分离工序包括：a)将升压后的含有IPA的废水供给到反渗透膜模块的步骤；以及b)将渗透过了反渗透膜模块的废水移送到渗透水箱的步骤，如图1的连续工序框图所示，首先，从IPA溶液箱100将含有IPA的废水经溶液过滤器210移送到IPA溶液高压泵220，将IPA溶液升压。此时，优选高压泵220的供给压力维持在10bar～70bar，如果以不足10bar运行，则推进力低，因此反渗透膜的渗透量大幅降低，如果超过70bar，则反渗透膜的长期稳定性降低，因此，调节成IPA溶液被高压泵220升压而维持在10bar～70bar。On the other hand, in the composite membrane separation method of the present invention, the reverse osmosis membrane separation process is carried out simultaneously, and the reverse osmosis membrane separation process of the above-mentioned II) step comprises: a) the waste water containing IPA after boosting is supplied to the reverse osmosis membrane module and b) the step of transferring the waste water that has penetrated the reverse osmosis membrane module to the permeation water tank, as shown in the continuous process block diagram of Figure 1, at first, the waste water containing IPA is passed through the solution filter 210 from the IPA solution tank 100 Transfer to the IPA solution high-pressure pump 220 to boost the pressure of the IPA solution. At this time, the supply pressure of the high-pressure pump 220 is preferably maintained at 10bar to 70bar. If it is operated at less than 10bar, the propulsive force will be low, so the permeation of the reverse osmosis membrane will be greatly reduced. If it exceeds 70bar, the long-term stability of the reverse osmosis membrane will be reduced. Therefore, it is adjusted so that the pressure of the IPA solution is boosted by the high-pressure pump 220 and maintained at 10 bar to 70 bar.
接着，将升压至10bar～70bar的IPA溶液经溶液流量计230供给到反渗透膜模块240，渗透过了反渗透膜模块240的废水经过渗透水流量计250而被移送到渗透水箱260。通过该反渗透膜分离工序而渗透的废水(渗透水)由于IPA的浓度为0.5％以下，所以不进行其它稀释而直接在废水处理厂进行处理即可。Next, the IPA solution boosted to 10bar to 70bar is supplied to the reverse osmosis membrane module 240 through the solution flowmeter 230 , and the wastewater permeated through the reverse osmosis membrane module 240 is transferred to the permeate water tank 260 through the permeate water flowmeter 250 . Wastewater (permeated water) permeated through this reverse osmosis membrane separation process has a concentration of IPA of 0.5% or less, so it may be treated in a waste water treatment plant without further dilution.
如以上说明，在实际进行图1所示的连续(continuous)复合膜分离方法中，将固定量的含有IPA的废水(IPA溶液)填充到箱100，使用渗透蒸发膜分离工序将IPA分离及浓缩，同时也一起进行反渗透膜分离工序，使水(废水)渗透而将其移送到渗透水箱260。此时，确认渗透蒸发膜分离工序的IPA浓缩液的量和反渗透膜分离工序的渗透水的量，对IPA溶液箱100连续地进行补充，根据要连续地处理的量(连续的废水产生量)来设计渗透蒸发膜分离工序和反渗透膜分离工序的容量，能够连续地运行这些工序。As explained above, in the actual continuous (continuous) composite membrane separation method shown in FIG. 1, a fixed amount of wastewater containing IPA (IPA solution) is filled into the tank 100, and the IPA is separated and concentrated using the pervaporation membrane separation process. At the same time, the reverse osmosis membrane separation process is also performed to permeate water (waste water) and transfer it to the permeate water tank 260 . Now, confirm the amount of the IPA concentrated solution of the pervaporation membrane separation process and the amount of permeate water in the reverse osmosis membrane separation process, the IPA solution tank 100 is continuously replenished, according to the amount to be continuously processed (continuous waste water production amount) ) to design the capacity of the pervaporation membrane separation process and the reverse osmosis membrane separation process, and these processes can be operated continuously.
另一方面，作为其它运行例，也能够进行图2所示的分批(batch)式的复合膜分离方法，将固定量的含有IPA的废水(IPA溶液)填充到箱100，在使用渗透蒸发膜分离工序将IPA分离及浓缩之后，当原来的含有IPA的废水的浓度降低到一定浓度以下时，将IPA溶液箱100的溶液移送到另一IPA溶液箱200，该移送了的含有IPA的废水通过反渗透膜分离工序使水渗透并贮存于渗透水箱260，从IPA溶液箱200的IPA溶液除去水，当IPA增加至一定浓度时被移送到IPA溶液箱100，再次进行渗透蒸发膜分离工序，通过重复运行上述工序而对含有IPA的废水全部处理，渗透水箱260的渗透水由于IPA的浓度降低，因此能够在废水处理厂进行处理。On the other hand, as another operation example, it is also possible to carry out the composite membrane separation method of batch (batch) formula shown in FIG. After the membrane separation process separates and concentrates IPA, when the concentration of the original waste water containing IPA drops below a certain concentration, the solution in the IPA solution tank 100 is transferred to another IPA solution tank 200, and the transferred waste water containing IPA Through the reverse osmosis membrane separation process, water is infiltrated and stored in the permeation water tank 260. Water is removed from the IPA solution in the IPA solution tank 200. When the IPA increases to a certain concentration, it is transferred to the IPA solution tank 100, and the pervaporation membrane separation process is performed again. By repeating the above steps, all the waste water containing IPA is treated, and the permeate water in the permeate water tank 260 can be treated in a waste water treatment plant because the concentration of IPA is reduced.
并且，虽然附图中未图示，但还能够进行下述半分批(semi－batch)式的复合膜分离方法：将固定量的含有IPA的废水(IPA溶液)填充到箱100，在使用渗透蒸发膜分离工序将IPA分离及浓缩的同时，也一起进行反渗透膜分离工序，使水(废水)渗透而将其移送到渗透水箱260，之后继续运行，当IPA溶液箱100的水平(level)成为一定量以下时，补充含有IPA的废水，根据IPA溶液箱100的上限及下限水平来以分批式运行。In addition, although not shown in the drawings, it is also possible to perform the following semi-batch composite membrane separation method: a fixed amount of wastewater containing IPA (IPA solution) is filled into the tank 100, and the tank 100 is filled with osmotic While the evaporation membrane separation process separates and concentrates IPA, it also performs the reverse osmosis membrane separation process together to permeate water (waste water) and transfer it to the permeation water tank 260, and then continue to run. When the level of the IPA solution tank 100 is When it becomes below a certain amount, waste water containing IPA is replenished, and it operates in batch mode according to the upper limit and lower limit levels of the IPA solution tank 100 .
另一方面，作为本发明的复合膜分离方法所包括的渗透蒸发膜分离工序的膜材料，优选为在聚醚酰亚胺等多孔性支承体涂覆了聚二甲基硅氧烷(PDMS)等有机聚硅氧烷的硅酮类复合膜，但不限于此。另外，作为反渗透膜分离工序的膜材料，优选在聚砜等多孔性支承体涂覆了聚酰胺的聚酰胺类复合膜，但不限于此。On the other hand, as the membrane material of the pervaporation membrane separation process included in the composite membrane separation method of the present invention, it is preferable to coat polydimethylsiloxane (PDMS) on a porous support such as polyetherimide. Silicone-based composite films of organopolysiloxanes, but not limited thereto. In addition, as the membrane material in the reverse osmosis membrane separation step, a polyamide-based composite membrane in which polyamide is coated on a porous support such as polysulfone is preferable, but not limited thereto.
具体实施方式 detailed description
以下，详细说明具体的实施例。Hereinafter, specific examples will be described in detail.
(实施例1)(Example 1)
将含有IPA的废水的IPA的浓度固定为5.2重量％，将供给流量固定为80LPM(literperminute，升每分钟)，使供给溶液的温度分别变化到35℃、45℃及55℃，进行图1所示的连续复合膜分离方法，表1示出按照渗透蒸发膜分离工序的供给溶液的温度的渗透溶液的IPA的浓度及渗透流量。The IPA concentration of the wastewater containing IPA is fixed at 5.2% by weight, the supply flow rate is fixed at 80LPM (liter per minute, liters per minute), the temperature of the supply solution is changed to 35°C, 45°C and 55°C respectively, and the process shown in Figure 1 is carried out. The continuous composite membrane separation method shown, Table 1 shows the concentration of IPA and the permeate flow rate of the permeate solution according to the temperature of the supply solution in the pervaporation membrane separation process.
[表1][Table 1]
(实施例2)(Example 2)
除了将含有IPA的废水的IPA的浓度固定为8.7重量％以外，以与实施例1相同的方法进行连续复合膜分离方法，表2示出按照渗透蒸发膜分离工序的供给溶液的温度的渗透溶液的IPA的浓度及渗透流量。Except that the concentration of IPA in the wastewater containing IPA was fixed at 8.7% by weight, the continuous composite membrane separation method was carried out in the same manner as in Example 1, and Table 2 shows the permeate solution according to the temperature of the supply solution in the pervaporation membrane separation process. The concentration of IPA and the permeate flow rate.
[表2][Table 2]
(实施例3)(Example 3)
将供给溶液的温度固定为35℃，将供给流量固定为20LPM，使含有IPA的废水的IPA的浓度分别变化成5.2重量％、6.2重量％、7.3重量％及8.5重量％，进行图1所示的连续复合膜分离方法，表3示出反渗透膜分离工序的渗透溶液(渗透水)的IPA的浓度及渗透流量。The temperature of the supply solution is fixed at 35°C, the supply flow rate is fixed at 20LPM, and the concentration of IPA in the wastewater containing IPA is changed to 5.2% by weight, 6.2% by weight, 7.3% by weight and 8.5% by weight respectively, and the process shown in Figure 1 is carried out. The continuous composite membrane separation method, table 3 shows the concentration and permeate flow of the IPA of the permeate solution (permeate water) of the reverse osmosis membrane separation process.
[表3][table 3]
如表1及表2所示，根据本发明的复合膜分离方法的实施例1及2的渗透蒸发膜分离工序，可知在供给溶液的温度相同的情况下，含有IPA的废水的IPA的浓度越高，渗透溶液的IPA的浓度及渗透流量越增加，此外，确认了在所有情况下，渗透溶液的IPA的浓度都示出38％以上，渗透溶液能够被回收再用。As shown in table 1 and table 2, according to the pervaporation membrane separation process of embodiment 1 and 2 of the composite membrane separation method of the present invention, it can be known that under the same situation of the temperature of the supply solution, the concentration of IPA in the wastewater containing IPA is higher. The higher the concentration of IPA in the permeate solution and the higher the permeate flow rate, it was confirmed that the concentration of IPA in the permeate solution was 38% or more in all cases, and the permeate solution could be recovered and reused.
并且，如表3所示，根据本发明的复合膜分离方法的实施例3的反渗透膜分离工序，当含有IPA的废水的IPA的浓度(供给溶液的浓度)从5.2重量％增加至8.5重量％时，渗透溶液(渗透水)的IPA的浓度稍微增加，渗透流量减少，但是在所有情况下，渗透溶液(渗透水)的IPA的浓度均不足0.5重量％，因此，确认了能够将渗透溶液(渗透水)直接移送到废水处理厂进行废水处理。And, as shown in table 3, according to the reverse osmosis membrane separation process of the embodiment 3 of the composite membrane separation method of the present invention, when the concentration of the IPA (concentration of the supply solution) of the waste water containing IPA increases from 5.2% by weight to 8.5% by weight %, the concentration of IPA in the permeate solution (permeate water) slightly increased, and the permeate flow rate decreased, but in all cases, the concentration of IPA in the permeate solution (permeate water) was less than 0.5% by weight. Therefore, it was confirmed that the permeate solution (permeate water) could (permeate water) is directly transferred to the wastewater treatment plant for wastewater treatment.
工业上的可利用性Industrial availability
因此，根据本发明的复合膜分离方法示出以下的显著的效果，即，能够从IPA清洗废水选择性地分离IPA，将其浓缩为30重量％以上来回收再用，并且，0.5重量％以下的低浓度的IPA清洗废水能够不进行其它稀释而在已有的废水处理厂直接进行处理。Therefore, according to the composite membrane separation method of the present invention, the following remarkable effects are shown, that is, IPA can be selectively separated from IPA cleaning wastewater, and it is concentrated to more than 30% by weight for recycling, and, 0.5% by weight or less The low-concentration IPA cleaning wastewater can be directly treated in the existing wastewater treatment plant without other dilution.
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| PCT/KR2014/008334 WO2015053483A1 (en) | 2013-10-07 | 2014-09-04 | Combined membrane separation process for concentrating ipa from wastewater containing ipa and treating wastewater |
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| JP2025143853A (en) * | 2024-03-19 | 2025-10-02 | 株式会社Ｓｃｒｅｅｎホールディングス | Organic solvent recovery device, substrate treatment device, and organic solvent recovery method |
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