CN105683092B - For carrying out IPA concentration and the compound membrane separating method of wastewater treatment to the waste water containing IPA - Google Patents
For carrying out IPA concentration and the compound membrane separating method of wastewater treatment to the waste water containing IPA Download PDFInfo
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- CN105683092B CN105683092B CN201480055455.1A CN201480055455A CN105683092B CN 105683092 B CN105683092 B CN 105683092B CN 201480055455 A CN201480055455 A CN 201480055455A CN 105683092 B CN105683092 B CN 105683092B
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- ipa
- waste water
- water containing
- reverse osmosis
- separating method
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- 239000012528 membrane Substances 0.000 title claims abstract description 76
- 239000002351 wastewater Substances 0.000 title claims abstract description 62
- 238000000034 method Methods 0.000 title claims abstract description 40
- 150000001875 compounds Chemical class 0.000 title claims abstract description 25
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 21
- 238000000926 separation method Methods 0.000 claims abstract description 46
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 34
- 230000003204 osmotic effect Effects 0.000 claims abstract description 26
- 238000001704 evaporation Methods 0.000 claims abstract description 25
- 230000008020 evaporation Effects 0.000 claims abstract description 25
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 claims description 276
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 238000001764 infiltration Methods 0.000 claims description 22
- 238000005373 pervaporation Methods 0.000 claims description 21
- 230000008595 infiltration Effects 0.000 claims description 20
- 239000002131 composite material Substances 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 239000007791 liquid phase Substances 0.000 claims description 5
- 229920002647 polyamide Polymers 0.000 claims description 4
- 229920001296 polysiloxane Polymers 0.000 claims description 3
- 239000004952 Polyamide Substances 0.000 claims description 2
- 229920002492 poly(sulfone) Polymers 0.000 claims description 2
- -1 dimethyl siloxane Chemical class 0.000 claims 1
- 239000012141 concentrate Substances 0.000 abstract description 5
- 238000010790 dilution Methods 0.000 abstract description 5
- 239000012895 dilution Substances 0.000 abstract description 5
- 239000000243 solution Substances 0.000 description 45
- 238000004140 cleaning Methods 0.000 description 7
- 238000010586 diagram Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 3
- 150000002894 organic compounds Chemical class 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000010534 mechanism of action Effects 0.000 description 2
- 230000035515 penetration Effects 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 230000001141 propulsive effect Effects 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 125000000118 dimethyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000005381 potential energy Methods 0.000 description 1
- XTUSEBKMEQERQV-UHFFFAOYSA-N propan-2-ol;hydrate Chemical compound O.CC(C)O XTUSEBKMEQERQV-UHFFFAOYSA-N 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000009738 saturating Methods 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 229920005573 silicon-containing polymer Polymers 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/08—Thin film evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/448—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by 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
- B01D61/58—Multistep processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
Abstract
The present invention relates to a kind of compound membrane separating method for being used to carry out the waste water containing IPA IPA concentration and wastewater treatment, it is more particularly to combine osmotic evaporation film separation circuit and reverse osmosis membrane separation process, can be separated from the waste water containing IPA and concentrate IPA while the compound membrane separating method of processing waste water.According to the compound membrane separating method of the present invention, it can be cleaned from IPA in waste water and be optionally sequestered IPA, it is concentrated into more than 30 weight % to recycle, directly handled in existing waste water treatment plant without other dilutions further, it is possible to which the IPA of below 0.5 weight % low concentration is cleaned into waste water.
Description
Technical field
The present invention relates to for containing IPA waste water carry out IPA concentration and wastewater treatment compound membrane separating method,
It is more particularly to combine osmotic evaporation film separation circuit and reverse osmosis membrane separation process, can be from the waste water containing IPA
Middle separation and concentration IPA are while the compound membrane separating method of processing waste water.
Background technology
IPA (isopropanol) is more as cleaning in industry workshop particularly semiconductor fabrication sequence and LCD manufacturing processes etc.
Solution is used, and the weight % of 5 weight %~15 IPA is usually contained in the cleaning waste water after the use.On so caused useless
Water, in terms of the recovery of organic compound especially alcohol, because IPA concentration is very low, using common
Distillation process does not have economy when being separated, concentrated, therefore there is currently the problem of wastewater treatment is all carried out to it.
On the other hand, waste water is cleaned on such IPA, in terms of wastewater treatment, because IPA concentration mistake
Height, so being diluted in the presence of with water, IPA concentration is set to be reduced to the other problems of less than 1% progress wastewater treatment.
It has been related to the first research (patent document 1,2) of osmotic evaporation film separation circuit, the pervaporation UF membrane work
Sequence is used to being optionally sequestered from the mixed solution of the alcohol such as IPA/water water using osmotic evaporation film or from organic compound water
Organic compound is optionally sequestered in solution, and the technology that waste water is handled using reverse osmosis membrane separation process is also widely known by the people
(patent document 3,4), but osmotic evaporation film separation circuit and reverse osmosis membrane separation process be according to purposes and characteristic respectively as
Different processes are carried out.
Therefore, the IPA of the concentration of wastewater treatment cleaning waste water is recycled or carries out for being unsuitable for being concentrated, such as
Fruit separates IPA using reverse osmosis membrane separation process in the lump and made while using osmotic evaporation film separation circuit to concentrate IPA
IPA concentration becomes suitable for the concentration of wastewater treatment, then can be selected from the conventional IPA cleaning waste water that all carry out wastewater treatment
Property separate and concentrate IPA to recycle, also, low concentration IPA cleaning waste water can without it is other dilution and
Some waste water treatment plants are directly handled, and present inventor is conceived to the above situation, complete the present invention.
Prior art literature
Patent document
Patent document 1：Japanese Laid-Open Patent Publication the 10-2011-0083077th；
Patent document 2：Japanese Laid-Open Patent Publication the 10-2000-0067454th；
Patent document 3：Japanese Laid-Open Patent Publication the 10-2013-0032294th；
Patent document 4：Japanese Laid-Open Patent Publication the 10-2005-0026294th.
The content of the invention
Problems to be solved by the invention
The present invention makes in view of the above-mentioned problems, and its object is to provide one kind to combine pervaporation UF membrane
The compound membrane separating method of process and reverse osmosis membrane separation process, it can be cleaned from IPA in waste water and be optionally sequestered IPA and incite somebody to action
It is concentrated into more than 30 weight % to recycle, and the IPA cleaning waste water of below 0.5 weight % low concentration can not enter
Row it is other dilution and directly handled in existing waste water treatment plant.
The solution used to solve the problem
In order to realize the purpose, the present invention provides a kind of compound membrane separating method, including：I osmotic evaporation film point) is passed through
From process from the waste water containing IPA the step of concentration IPA；And II) by reverse osmosis membrane separation process from useless containing IPA
The step of water process waste water.
Characterized in that, the I) the osmotic evaporation film separation circuit of step includes：I) what be will heat up is useless containing IPA
Water is supplied to the step of pervaporation film module；Ii) IPA for having penetrated pervaporation film module is condensed into the step of liquid phase
Suddenly；And iii) the step of curdy IPA is transplanted on percolating solution case.
Characterized in that, the waste water containing IPA to have heated up maintains 30 DEG C~60 DEG C by heater.
Characterized in that, the supply flow rate for being supplied to the waste water containing IPA of the pervaporation film module is osmotic flow
More than 5 times of amount.
Characterized in that, the II) the reverse osmosis membrane separation process of step includes：A) it is useless containing IPA by what is boosted
Water is supplied to the step of reverse osmosis membrane module；And the move wastewater of reverse osmosis membrane module will b) have been penetrated to infiltration water tank
Step.
Characterized in that, the waste water containing IPA to have boosted maintains 10bar~70bar by high-pressure pump.
Characterized in that, the supply flow rate for being supplied to the waste water containing IPA of the reverse osmosis membrane module is seepage discharge
More than 3 times.
Invention effect
According to the compound membrane separating method of the present invention, it can be cleaned from IPA in waste water and be optionally sequestered IPA, its is dense
It is reduced to more than 30 weight % to recycle, while the IPA of the low concentration below 0.5 weight % can be cleaned into waste water not
Carry out other dilutions and directly handled in existing waste water treatment plant.
Brief description of the drawings
Fig. 1 is the block diagram for showing continous way (continuous) compound membrane separating method of the present invention；
Fig. 2 is the block diagram for showing batch-type (batch) compound membrane separating method of the present invention.
Embodiment
Hereinafter, describe the present invention in detail concentrates IPA while using counter-infiltration using osmotic evaporation film separation circuit
UF membrane process separates IPA so that IPA concentration is suitable to the compound membrane separating method and accompanying drawing of the concentration of wastewater treatment.
The present invention provides a kind of compound membrane separating method, including：I) by osmotic evaporation film separation circuit from containing IPA's
The step of IPA is concentrated in waste water；And II) by reverse osmosis membrane separation process from the wastewater treatment waste water containing IPA the step of.
In addition, above-mentioned I) the osmotic evaporation film separation circuit of step includes：I) supply of the waste water containing IPA that will heat up
The step of to pervaporation film module；Ii the step of IPA for having penetrated pervaporation film module) is condensed into liquid phase；And
Iii the step of curdy IPA) is transplanted on percolating solution case, as shown in Fig. 1 continuous (continuous) process block diagram,
First, the waste water (IPA solution) containing IPA is stored in IPA liquor boxs 100, utilizes the common heating unit such as heater 110
The IPA solution of IPA liquor boxs is set to heat up.Now, if the temperature of IPA solution is less than 30 DEG C, pervaporation film module oozes
Penetration is too small, if the temperature of IPA solution, more than 60 DEG C, energy expenditure is excessive, it is therefore preferable that IPA solution passes through heater
110 heat up and maintain 30 DEG C~60 DEG C.
Then, will heat up to 30 DEG C~60 DEG C of IPA solution and be supplied to pervaporation film module 150, here, along with according to
The secondary process by IPA solution supply pump 120, solution strainer 130 and IPA liquid inventories meter 140.Now, it is preferably fed to
The supply flow rate of the IPA solution of pervaporation film module 150 is adjusted to more than 5 times of seepage discharge.If by IPA solution to ooze
Less than 5 times of saturating flow are supplied to pervaporation film module 150, then the percolating solution permeated by pervaporation film module 150
IPA concentration it is low, it is thus impossible to swimmingly be separated and concentrated.
There is the IPA solution for being supplied to pervaporation film module 150 like this IPA to be dissolved in seperation film, in seperation film
It is interior diffusion and with the mechanism of action of gas-phase permeation.According to this mechanism of action, one end and the IPA of pervaporation film module 150 are supplied
Contacted to solution, the steam press contacts of the other end and low penetrant, low vapour pressure condition can be by vacuumizing or making
Inert carrier gas is flowed into and generated.Therefore, generally, it is internally generated as pushing away for osmotic evaporation film separation circuit in osmotic evaporation film
Enter the gradient of the chemical potential energy of power (driving force), carry out infiltration of the material via film, therefore, in the present invention, in order to
The propulsive force of osmotic evaporation film separation circuit is maintained, osmosizing portion is maintained vacuum by using vavuum pump 170.
Secondly, the IPA for having penetrated the gas phase of pervaporation film module 150 is condensed into liquid phase in common condenser 160,
The IPA of curdy liquid phase is shifted into percolating solution case 190 by percolating solution flowmeter 180.Pass through the pervaporation
The IPA solution that UF membrane process obtains is concentrated into more than 30%, therefore can be recovered for re-use.
On the other hand, reverse osmosis membrane separation process, above-mentioned II are carried out simultaneously in the compound membrane separating method of the present invention) step
Rapid reverse osmosis membrane separation process includes：A) the step of waste water containing IPA after boosting being supplied to reverse osmosis membrane module；With
And will b) the step of move wastewater of reverse osmosis membrane module is to infiltration water tank have been penetrated, as shown in Fig. 1 series-operation block diagram,
First, IPA solution high-pressure pump 220 is transplanted on through solution strainer 210 from IPA liquor boxs 100 by the waste water containing IPA, by IPA
Solution boosts.Now, the supply pressure of preferably high-pressure pump 220 maintains 10bar~70bar, if to be run less than 10bar,
Then propulsive force is low, therefore the infiltration capacity of reverse osmosis membrane is greatly reduced, if it exceeds 70bar, then reverse osmosis membrane long-time stability
Reduce, therefore, be adjusted to IPA solution and boosted by high-pressure pump 220 and maintain 10bar~70bar.
Then, the IPA solution for boosting to 10bar~70bar is supplied to reverse osmosis membrane module through liquid inventory meter 230
240, the waste water for having penetrated reverse osmosis membrane module 240 is shifted into infiltration water tank 260 by infiltration water ga(u)ge 250.It is logical
The waste water (infiltration water) crossed the reverse osmosis membrane separation process and permeated is because IPA concentration is less than 0.5%, so without it
It dilutes and directly handled in waste water treatment plant.
It is as described above, in continuous (continuous) the compound membrane separating method shown in Fig. 1 is actually carried out, by fixation
The waste water (IPA solution) containing IPA of amount is filled into case 100, and IPA is separated and concentrated using osmotic evaporation film separation circuit,
Also carry out reverse osmosis membrane separation process together simultaneously, permeate water (waste water) and be transplanted on infiltration water tank 260.Now, really
The amount of the IPA concentrates of osmotic evaporation film separation circuit and the amount of the infiltration water of reverse osmosis membrane separation process are recognized, to IPA liquor boxs
100 are continuously supplemented, and pervaporation UF membrane is designed according to the amount (continuous waste water yield) continuously to handle
The capacity of process and reverse osmosis membrane separation process, it can continuously run these processes.
On the other hand, as other operation examples, the compound UF membrane of (batch) in batches formula shown in Fig. 2 can also be carried out
Method, the waste water (IPA solution) containing IPA of fixed amount is filled into case 100, will in use osmotic evaporation film separation circuit
After IPA is separated and concentrated, when the concentration of the original waste water containing IPA is reduced to below finite concentration, by IPA liquor boxs
100 solution is transplanted on another IPA liquor boxs 200, and the waste water containing IPA transferred is made by reverse osmosis membrane separation process
Water penetration is simultaneously stored in infiltration water tank 260, water is removed from the IPA solution of IPA liquor boxs 200, when IPA increases to finite concentration
Be shifted into IPA liquor boxs 100, again carry out osmotic evaporation film separation circuit, by rerun above-mentioned operation and to containing
IPA waste water is all handled, and the infiltration water of infiltration water tank 260 can be entered due to IPA concentration reduction in waste water treatment plant
Row processing.
Although also, it is not shown in accompanying drawing, the composite membrane point of following semi-batch (semi-batch) formula can also be carried out
From method：The waste water (IPA solution) containing IPA of fixed amount is filled into case 100, will in use osmotic evaporation film separation circuit
While IPA is separated and concentrated, reverse osmosis membrane separation process is also carried out together, water (waste water) is permeated and is transplanted on infiltration
Water tank 260, is continued to run with afterwards, and when the level (level) of IPA liquor boxs 100 turns into a certain amount of following, supplement contains IPA
Waste water, run according to the upper limit of IPA liquor boxs 100 and threshold level with batch-type.
On the other hand, the membrane material as the osmotic evaporation film separation circuit included by the compound membrane separating method of the present invention
Material, is preferably coated with the organopolysiloxanes such as dimethyl silicone polymer (PDMS) in the porous supporting mass such as PEI
Silicone composite membrane, but not limited to this.In addition, the membrane material as reverse osmosis membrane separation process, preferably in porous such as polysulfones
Supporting mass is coated with the polyamide-based composite membrane of polyamide, but not limited to this.
Embodiment
Hereinafter, specific embodiment is described in detail.
(embodiment 1)
The IPA of waste water containing IPA concentration is fixed as 5.2 weight %, supply flow rate is fixed as 80LPM (liter
Per minute, Liter Per Minute), the temperature of supply solution is changed to 35 DEG C, 45 DEG C and 55 DEG C respectively, carry out shown in Fig. 1
Continuous compound membrane separating method, table 1 show the percolating solution of the temperature of the supply solution according to osmotic evaporation film separation circuit
IPA concentration and seepage discharge.
[table 1]
(embodiment 2)
In addition to the IPA of the waste water containing IPA concentration is fixed as into 8.7 weight %, with side same as Example 1
Method carries out continuous compound membrane separating method, and table 2 shows the infiltration of the temperature of the supply solution according to osmotic evaporation film separation circuit
The IPA of solution concentration and seepage discharge.
[table 2]
(embodiment 3)
The temperature for supplying solution is fixed as 35 DEG C, supply flow rate is fixed as 20LPM, makes the IPA of the waste water containing IPA
Concentration be changing into 5.2 weight %, 6.2 weight %, 7.3 weight % and 8.5 weight % respectively, carry out continuous multiple shown in Fig. 1
Membrane separating method is closed, table 3 shows the IPA of the percolating solution (infiltration water) of reverse osmosis membrane separation process concentration and seepage discharge.
[table 3]
As shown in table 1 and table 2, according to the pervaporation UF membrane of the embodiment 1 and 2 of the compound membrane separating method of the present invention
Process, it is known that in the case of the temperature identical of supply solution, the IPA of the waste water containing IPA concentration is higher, percolating solution
IPA concentration and seepage discharge more increases, in addition, it is thus identified that in all cases, the IPA of percolating solution concentration shows that
More than 38%, percolating solution can be recovered for re-use.
Also, as shown in table 3, according to the present invention compound membrane separating method embodiment 3 reverse osmosis membrane separation process,
When the IPA of the waste water containing IPA concentration (concentration of supply solution) increases to 8.5 weight % from 5.2 weight %, infiltration is molten
The IPA of liquid (infiltration water) concentration somewhat increases, and seepage discharge is reduced, but in all cases, percolating solution (infiltration water)
IPA concentration less than 0.5 weight %, it is thus identified that percolating solution (infiltration water) can be transplanted directly at waste water
Manage factory and carry out wastewater treatment.
Industrial utilizability
Therefore, following significant effect is shown according to the compound membrane separating method of the present invention, i.e. can be cleaned from IPA
Separate IPA waste water selective, concentrated and recycled for more than 30 weight %, also, below 0.5 weight %'s is low dense
The IPA cleanings waste water of degree can directly be handled without other dilutions in existing waste water treatment plant.
Claims (3)
1. a kind of compound membrane separating method, including：
I the step of isopropanol (IPA)) is concentrated from the waste water containing isopropanol (IPA) by osmotic evaporation film separation circuit；With
And
II) by reverse osmosis membrane separation process from the wastewater treatment waste water containing isopropanol (IPA) the step of,
Wherein, the I) the osmotic evaporation film separation circuit of step includes：
I) the step of waste water containing isopropanol (IPA) that will heat up is supplied to pervaporation film module；
Ii the step of isopropanol (IPA) for having penetrated pervaporation film module) is condensed into liquid phase；And
Iii the step of curdy isopropanol (IPA)) is transplanted on percolating solution case,
The II) the reverse osmosis membrane separation process of step includes：
A) waste water containing isopropanol (IPA) by the boosting that 10bar~70bar is maintained by high-pressure pump is supplied to counter-infiltration
The step of film module；And
B) the step of move wastewater of reverse osmosis membrane module is to infiltration water tank will have been penetrated,
Wherein, the supply flow rate for being supplied to the waste water containing isopropanol (IPA) of the pervaporation film module is seepage discharge
More than 5 times, and
Wherein, the membrane material in the osmotic evaporation film separation circuit is poly- to be coated with the porous supporting mass of PEI
The silicone composite membrane of dimethyl siloxane, and the membrane material in the reverse osmosis membrane separation process is the porous in polysulfones
Supporting mass is coated with the polyamide-based composite membrane of polyamide.
2. compound membrane separating method as claimed in claim 1, it is characterised in that
The waste water containing isopropanol (IPA) to have heated up maintains 30 DEG C~60 DEG C by heater.
3. compound membrane separating method as claimed in claim 1, it is characterised in that
Be supplied to the supply flow rate of the waste water containing isopropanol (IPA) of the reverse osmosis membrane module for 3 times of seepage discharge with
On.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| KR1020130118983A KR101695215B1 (en) | 2013-10-07 | 2013-10-07 | Combined membrane separation process for concentration of IPA and treatment of wastewater from IPA-containing wastewater |
| KR10-2013-0118983 | 2013-10-07 | ||
| 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 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105683092A CN105683092A (en) | 2016-06-15 |
| CN105683092B true CN105683092B (en) | 2018-04-03 |
Family
ID=52813271
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201480055455.1A Active CN105683092B (en) | 2013-10-07 | 2014-09-04 | For carrying out IPA concentration and the compound membrane separating method of wastewater treatment to the waste water containing IPA |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JP6235133B2 (en) |
| KR (1) | KR101695215B1 (en) |
| CN (1) | CN105683092B (en) |
| WO (1) | WO2015053483A1 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20210082711A (en) * | 2019-12-26 | 2021-07-06 | 주식회사 에너엔비텍 | Pervaporation membrane separation process for concentration of the organic compound and treatment of wastewater from specific organic compound containing wastewater |
| CN113943209B (en) * | 2020-08-28 | 2023-05-23 | 苏州智程半导体科技股份有限公司 | Method and device for purifying isopropanol waste liquid |
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| US5989426A (en) * | 1995-07-05 | 1999-11-23 | Nitto Denko Corp. | Osmosis membrane |
| CN101351252A (en) * | 2005-12-29 | 2009-01-21 | 巴斯夫欧洲公司 | A process for separating propylene glycol from aqueous compositions |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58166901A (en) * | 1982-03-29 | 1983-10-03 | Kuri Kagaku Sochi Kk | Osmotic evaporation membrane and separation using said membrane |
| JPS61257205A (en) * | 1985-05-10 | 1986-11-14 | Agency Of Ind Science & Technol | Permselective membrane for alcohol and separation of alcohol using the same |
| DE3679990D1 (en) * | 1986-07-29 | 1991-08-01 | Gft Ges Fuer Trenntechnik | PERVAPORATION METHOD AND MEMBRANE. |
| US4944882A (en) * | 1989-04-21 | 1990-07-31 | Bend Research, Inc. | Hybrid membrane separation systems |
| TW224058B (en) * | 1990-12-27 | 1994-05-21 | Mitsubishi Chemicals Co Ltd | |
| JPH06292819A (en) * | 1993-04-09 | 1994-10-21 | Hitachi Chem Co Ltd | Treatment of phenols-containg waste liquid with pervaporation method and device there for |
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| Publication number | Publication date |
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| WO2015053483A1 (en) | 2015-04-16 |
| JP6235133B2 (en) | 2017-11-22 |
| CN105683092A (en) | 2016-06-15 |
| KR20150040455A (en) | 2015-04-15 |
| KR101695215B1 (en) | 2017-01-11 |
| JP2016532542A (en) | 2016-10-20 |
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