CN111603939A - System and method for concentrating organic solvent - Google Patents
System and method for concentrating organic solvent Download PDFInfo
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- CN111603939A CN111603939A CN202010370649.8A CN202010370649A CN111603939A CN 111603939 A CN111603939 A CN 111603939A CN 202010370649 A CN202010370649 A CN 202010370649A CN 111603939 A CN111603939 A CN 111603939A
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- 239000003960 organic solvent Substances 0.000 title claims abstract description 70
- 238000000034 method Methods 0.000 title claims abstract description 23
- 239000012528 membrane Substances 0.000 claims abstract description 72
- 239000000243 solution Substances 0.000 claims abstract description 60
- 238000009292 forward osmosis Methods 0.000 claims abstract description 53
- 239000002994 raw material Substances 0.000 claims abstract description 48
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 20
- 230000003204 osmotic effect Effects 0.000 claims abstract description 18
- 230000008595 infiltration Effects 0.000 claims abstract description 14
- 238000001764 infiltration Methods 0.000 claims abstract description 14
- 239000012141 concentrate Substances 0.000 claims abstract description 6
- 238000010790 dilution Methods 0.000 claims abstract description 3
- 239000012895 dilution Substances 0.000 claims abstract description 3
- 238000001223 reverse osmosis Methods 0.000 claims description 30
- 238000000605 extraction Methods 0.000 claims description 28
- 239000007788 liquid Substances 0.000 claims description 21
- 239000012466 permeate Substances 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 9
- 238000000909 electrodialysis Methods 0.000 claims description 7
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 6
- 230000004907 flux Effects 0.000 claims description 6
- 230000008569 process Effects 0.000 claims description 4
- 238000011084 recovery Methods 0.000 claims description 4
- 230000014759 maintenance of location Effects 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- 239000011780 sodium chloride Substances 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 230000008901 benefit Effects 0.000 abstract description 4
- 230000003670 easy-to-clean Effects 0.000 abstract description 3
- 238000005086 pumping Methods 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract 1
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000010923 batch production Methods 0.000 description 3
- 238000010924 continuous production Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000001728 nano-filtration Methods 0.000 description 3
- 238000002207 thermal evaporation Methods 0.000 description 3
- 150000002500 ions Chemical class 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000000149 chemical water pollutant Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000003014 ion exchange membrane Substances 0.000 description 1
- 230000037427 ion transport Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- 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
-
- 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
- B01D61/002—Forward osmosis or direct 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
- B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
- B01D61/422—Electrodialysis
-
- 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
- B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
- B01D61/44—Ion-selective electrodialysis
-
- 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
- B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
- B01D61/44—Ion-selective electrodialysis
- B01D61/46—Apparatus therefor
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- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Urology & Nephrology (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention relates to a system and a method for concentrating an organic solvent, which comprises a forward osmosis component and a concentration osmosis component; the positive osmotic subassembly is including having the positive osmotic membrane of resistant organic solvent function, set up in raw materials side input and the raw materials side output of positive osmotic membrane raw materials side, set up in the infiltration side output and the infiltration side input of positive osmotic membrane infiltration side, the organic solvent of treating the concentration of input on the raw materials side input, the organic solvent after the raw materials side output is concentrated, the extract after dilution of infiltration side output will be exported is imported to concentrated osmotic subassembly in, concentrated osmotic subassembly will concentrate the extract after input to the infiltration input. The organic solvent is concentrated through the forward osmosis membrane, the water of the organic solvent is extracted through the extracting solution, and meanwhile, the extracting solution is concentrated to realize recycling. The raw materials can be separated only by pumping into a forward osmosis membrane, so that the organic solvent is concentrated and is easy to clean; the system and the method have the advantages of extremely low energy consumption and improved use safety.
Description
Technical Field
The invention relates to the technical field of organic solvent concentration, in particular to a system and a method for concentrating an organic solvent.
Background
The organic solvent concentration process comprises three methods, namely a high-temperature thermal evaporation method, a high-pressure nanofiltration method and a high-pressure reverse osmosis method, and the high-temperature thermal evaporation method is commonly adopted at present, and concentration and purification are realized by utilizing different evaporation temperatures of different components.
Forward Osmosis (FO) is different from traditional external pressure driven membrane technologies (such as Reverse Osmosis (RO) and Nanofiltration (NF)), the FO is a natural osmosis process driven only by osmotic pressure, external pressure is not needed, energy consumption is extremely low, the polluted forward osmosis membrane is easy to clean, the service life is long, and the operation cost is low. The forward osmosis technology is applied to the separation and production process of special materials such as food, medicine, fine chemical engineering and the like, and the treatment of landfill leachate, industrial high-difficulty wastewater and the like, and has remarkable technical advantages and economic benefits.
Currently, there is a need for a concentration method of organic solvent that can reduce energy consumption and cost.
Disclosure of Invention
To achieve the above objects, a system and method for concentrating an organic solvent are provided.
The technical scheme adopted by the invention for solving the technical problems is as follows: a system for concentrating an organic solvent is characterized by comprising a forward osmosis component and a concentration osmosis component, wherein the forward osmosis component is used for concentrating the organic solvent, and the concentration osmosis component is used for concentrating an extracting solution; the positive osmotic subassembly including having the positive osmotic membrane of resistant organic solvent function, set up in the raw materials side input and the raw materials side output of positive osmotic membrane raw materials side, set up in the infiltration side output and the infiltration side input of positive osmotic membrane infiltration side the raw materials side input on input the organic solvent of treating the concentration, raw materials side output concentrated organic solvent, the extraction liquid after will exporting input to concentrated osmotic subassembly in with the dilution, concentrated osmotic subassembly input to the infiltration input after will concentrating, concentrated osmotic subassembly after the separation water output.
More specifically, the concentration and permeation component concentrates the extracting solution through high-pressure reverse osmosis.
More specifically, the concentration and permeation assembly comprises a reverse osmosis membrane for concentrating an extracting solution, an extracting side input end and an extracting side output end which are arranged on the extracting solution side of the reverse osmosis membrane, and a separation output end which is arranged on the permeation side of the reverse osmosis membrane, wherein the extracting side input end is communicated with the permeation side output end, and the extracting side output end is communicated with the permeation side input end; a supercharging device is arranged at the input end of the extraction side.
More specifically, the concentration and permeation module adopts an electrodialysis technology to concentrate the extracting solution.
More specifically, the raw material side input end and the raw material side output end are connected with a raw material liquid barrel; the permeation input end, the permeation output end, the extraction side input end and the extraction side output end are connected with an extraction liquid barrel, and the separation output end is connected with a pure water recovery barrel.
Further specifically, the raw material side input end is connected with a raw material liquid barrel, the raw material side output end is connected with a concentrated organic solution barrel, the permeation input end and the extraction side output end are connected with a concentrated extraction liquid barrel, and the permeation output end and the extraction side input end are connected with a diluted extraction liquid barrel.
A process for concentrating an organic solvent comprising the steps of,
a) concentrating an organic solution, namely introducing a low-concentration organic solvent to one side of a forward osmosis membrane resistant to the organic solvent, introducing an extracting solution to the other side of the forward osmosis membrane, taking the concentration difference of two sides of the forward osmosis membrane as a driving force, and allowing water molecules of the organic solvent to pass through the forward osmosis membrane to extract the organic solvent to be high-concentration;
b) and (3) concentrating the extracting solution, wherein the high-concentration extracting solution passes through the forward osmosis membrane to be changed into a low-concentration extracting solution, the low-concentration extracting solution is changed into a high-concentration extracting solution in a high-pressure reverse osmosis or electrodialysis mode, and the high-concentration extracting solution is returned to the forward osmosis membrane for continuous use.
More specifically, in the step b), the high-pressure reverse osmosis mode is to introduce a low-concentration extracting solution to one side of the reverse osmosis membrane, discharge water molecules in the low-concentration extracting solution through the other side of the reverse osmosis membrane by increasing the pressure, change the extracting solution into high concentration, and continuously introduce the high-concentration extracting solution into the forward osmosis membrane.
More specifically, the forward osmosis membrane selects and concentrates 5% of DMF organic solvent under the condition that the extracting solution is 1M NaCl solution, and the water flux of the forward osmosis membrane is 1-10L/M2Hr, reverse salt flux 0.1-5g/m2Per hr, the retention rate of the organic solvent is more than 80%.
The invention has the beneficial effects that: by adopting the natural permeation function of the forward osmosis membrane resistant to the organic solvent, the raw material can be separated only by pumping the raw material into the forward osmosis membrane, so that the concentration of the organic solvent can be realized, and the forward osmosis membrane is easy to clean; the extract can be recycled in a high-pressure reverse osmosis or electrodialysis mode; the system and the method have the advantages of extremely low energy consumption, easy cleaning of the forward osmosis membrane, simple structure, convenient use, no high-temperature potential safety hazard and improved use safety.
Drawings
FIG. 1 is a schematic diagram of the system for concentrating organic solvents according to the present invention;
FIG. 2 is a schematic diagram of a system architecture for small batch production of the present invention;
fig. 3 is a schematic diagram of the system structure for mass continuous production of the present invention.
In the figure: 1. a forward osmosis membrane; 2. a reverse osmosis membrane; 3. a raw material liquid barrel; 4. an extraction liquid barrel; 5. a pure water recovery barrel; 6. a pressure boosting device; 7. concentrating the extract barrel; 8. a concentrated organic solvent barrel; 9. a barrel for diluting the extraction solution; 11. a raw material side input end; 12. a raw material side output end; 13. a permeate side output; 14. a permeate side input; 21. an extraction side input; 22. an extraction side output end; 23. and separating the output end.
Detailed Description
The invention is described in detail below with reference to the figures and the detailed description.
Because the current osmotic membrane cannot tolerate organic solvent, the concentration mode of the organic solvent is limited, and the membrane material with the function of tolerating the organic solvent is adopted in the schemeTo form a forward osmosis membrane; taking 5% DMF (dimethylformamide) water solution as an example for concentration, and 1M NaCl solution as an extracting solution, the water flux of the forward osmosis membrane is 1-10L/M2Hr, reverse salt flux 0.1-5g/m2The retention rate of the organic solvent is more than 80 percent.
Based on the forward osmosis membrane, a method for organic solvents is designed, which comprises the following steps,
a) the concentration of the organic solution is to introduce a low-concentration organic solvent into one side of the forward osmosis membrane 1, and to introduce an extracting solution into the other side of the forward osmosis membrane 1, wherein the concentration of the extracting solution is greater than that of the organic solvent, the purpose is to enable concentration difference to appear on two sides of the forward osmosis membrane 1, and the concentration difference is used as a driving force, the forward osmosis membrane 1 only enables water molecules in the organic solvent to pass through, the water molecules of the organic solvent enter the extracting solution after passing through the forward osmosis membrane 1, at the moment, the moisture in the organic solvent is reduced to become the high-concentration organic solvent, and the moisture in the extracting solution is increased to become the low-concentration extracting.
b) And (3) concentrating the extracting solution, wherein the extracting solution with low concentration is changed into the extracting solution with high concentration by means of high-pressure reverse osmosis or electrodialysis, water molecules in the extracting solution with low concentration are extracted, the extracting solution is changed into high concentration and returns to the forward osmosis membrane 1 for continuous use, and the separated water can be directly discharged.
The electrodialysis is carried out by means of ion-exchange membranes, which, during their ion transport, pass the ions if their fixed charge is opposite to that of the ions, and repel them if their charge is the same, in such a way that a concentration of the extraction liquid is achieved.
In this scheme, the concentration of extract adopts high pressure reverse osmosis's mode to extract, lets in the extract of low concentration to reverse osmosis membrane 2 one side, and the opposite side behind reverse osmosis membrane 2 is discharged through increasing pressure with the hydrone in the extract of low concentration, and the extract becomes high concentration.
A system for concentrating an organic solvent, which is designed based on the above method as shown in FIG. 1, includes a forward osmosis module for concentrating an organic solvent and a concentration osmosis module for concentrating an extraction solution, the forward osmosis component comprises a forward osmosis membrane 1 with the function of resisting organic solvent, a raw material side input end 11 and a raw material side output end 12 which are arranged at the raw material side of the forward osmosis membrane 1, a permeation side output end 13 and a permeation side input end 14 which are arranged at the permeation side of the forward osmosis membrane 1, the organic solvent to be concentrated is input to the raw material side input end 11, the concentrated organic solvent is output from the raw material side output end 12, the output end 13 at the permeation side inputs the output diluted extracting solution into the concentration permeation component, the concentration and permeation component inputs the concentrated extracting solution to the permeation side input end 14, and the water separated by the concentration and permeation component is output.
In the scheme, a concentration and permeation component is designed in a high-pressure reverse osmosis mode, the concentration and permeation component comprises a reverse osmosis membrane 2 for concentrating an extracting solution, an extracting side input end 21 and an extracting side output end 22 which are arranged on an extracting solution side of the reverse osmosis membrane 2, and a separation output end 23 which is arranged on a permeation side of the reverse osmosis membrane 2, wherein the extracting side input end 21 is communicated with a permeation side output end 13, and the extracting side output end 22 is communicated with a permeation side input end 14; draw side input 21 department set up supercharging device 6, supercharging device 6 is used for increasing the pressure that the extract acted on reverse osmosis membrane 2, conveniently separates fast.
Based on the structure, the system can have two structural modes, and is suitable for small-batch production or large-batch continuous production respectively.
When the organic solvent is produced in small batches as shown in fig. 2, a raw material liquid barrel 3 is connected to the raw material side input end 11 and the raw material side output end 12, and the raw material liquid barrel 3 is simultaneously connected to the raw material side input end 11 and the raw material side output end 12; the permeate input end 14, the permeate output end 13, the extraction side input end 21 and the extraction side output end 22 are connected with an extraction liquid barrel 4, the extraction liquid barrel 4 is simultaneously connected with the permeate input end 14, the permeate output end 13, the extraction side input end 21 and the extraction side output end 22, and the separation output end 23 is connected with a pure water recovery barrel 5; the small-batch production is one-time production, when in use, the raw material liquid barrel 3 is inserted into the raw material side input end 11 and the raw material side output end 12, and the raw material liquid is conveyed to the forward osmosis membrane 1 through a pump, and the timing and the metering can be realized through a flow control valve; the system realizes the concentration of the organic solvent after the circulation is finished, the concentrated organic solvent is still stored in the raw material liquid barrel 3, the extracting solution in the corresponding extracting solution barrel 4 is recycled, the extracting solution is also conveyed by a pump, and the timing and the metering are carried out by a flow control valve.
As shown in fig. 3, when the organic solvent is continuously produced in a large scale, the raw material side input end 11 is connected with a raw material liquid barrel 3, the raw material side output end 12 is connected with a concentrated organic solvent barrel 8, the concentrated extract barrel 7 is connected between the osmosis input end 14 and the extraction side output end 22, the diluted extract barrel 9 is connected between the osmosis output end 13 and the extraction side input end 21, when the continuous production in a large scale is carried out, the liquids in the barrels are not mixed, the timing and metering at the position are controlled by a flow electromagnetic valve, the raw material liquid is sent to the position of the forward osmosis membrane 1 by a pump, and the extract is sent to the position of the reverse osmosis membrane 2.
In conclusion, by using the method and the system, the raw materials can be separated only by pumping into the forward osmosis membrane through the characteristic of the forward osmosis membrane 1, so that the energy consumption can be reduced, and the cost can be reduced; the concentration of the extracting solution is concentrated, so that the extracting solution can be repeatedly used, and the extracting solution is saved; meanwhile, the system can be continuously used, is simple and convenient to use, and improves the production efficiency; meanwhile, a high-temperature thermal evaporation method is not adopted, so that high-temperature risks can be reduced, and the production safety is improved.
It is to be emphasized that: the above embodiments are only preferred embodiments of the present invention, and are not intended to limit the present invention in any way, and all simple modifications, equivalent changes and modifications made to the above embodiments according to the technical spirit of the present invention are within the scope of the technical solution of the present invention.
Claims (9)
1. A system for concentrating an organic solvent is characterized by comprising a forward osmosis component and a concentration osmosis component, wherein the forward osmosis component is used for concentrating the organic solvent, and the concentration osmosis component is used for concentrating an extracting solution; the forward osmosis module including have positive osmotic membrane (1) of nai organic solvent function, set up in raw materials side input (11) and raw materials side output (12) of forward osmotic membrane (1) raw materials side, set up in infiltration side output (13) and infiltration side input (14) of forward osmotic membrane (1) infiltration side raw materials side input (11) on input the organic solvent of treating the concentration, raw materials side output (12) output the organic solvent after the concentration, infiltration side output (13) with the extract input to the concentrated osmosis module after the dilution of output in, the concentrated osmosis module with the extract after the concentration input to infiltration input (14), the water output after the separation of concentrated osmosis module.
2. The system for concentrating organic solvents according to claim 1, wherein the concentration and permeation module concentrates the extraction fluid by high pressure reverse osmosis.
3. The system for concentrating an organic solvent according to claim 2, wherein the concentration and permeation module comprises a reverse osmosis membrane (2) for concentrating the extract, an extract side input (21) and an extract side output (22) provided on the extract side of the reverse osmosis membrane (2), and a separation output (23) provided on the permeate side of the reverse osmosis membrane (2), wherein the extract side input (21) is communicated with the permeate side output (13), and the extract side output (22) is communicated with the permeate side input (14); a pressure boosting device (6) is arranged at the input end (21) of the extraction side.
4. A system for concentrating organic solvents according to claim 3, wherein the concentration permeate module employs electrodialysis to concentrate the extract.
5. A system for concentrating organic solvents according to claim 3, wherein a feed barrel (3) is connected to the feed side input (11) and the feed side output (12); the permeate input end (14), the permeate output end (13), the extraction side input end (21) and the extraction side output end (22) are connected with an extraction liquid barrel (4), and the separation output end (23) is connected with a pure water recovery barrel (5).
6. A system for concentrating organic solvents according to claim 3, wherein the feed side input (11) is connected to a feed liquid drum (3), the feed side output (12) is connected to a concentrated organic solution drum (8), the permeate input (14) and the extract side output (22) are connected to a concentrated extract drum (7), and the permeate output (13) and the extract side input (21) are connected to a dilute extract drum (9).
7. A process for concentrating an organic solvent, characterized by the steps of,
a) concentrating the organic solution, namely introducing a low-concentration organic solvent to one side of a forward osmosis membrane (1) resistant to the organic solvent, introducing an extracting solution to the other side of the forward osmosis membrane (1), taking the concentration difference of two sides of the forward osmosis membrane (1) as a driving force, and allowing water molecules of the organic solvent to pass through the forward osmosis membrane (1) to extract the organic solvent to be high in concentration;
b) and (3) concentrating the extracting solution, wherein the high-concentration extracting solution passes through the forward osmosis membrane (1) to be changed into a low-concentration extracting solution, the low-concentration extracting solution is changed into a high-concentration extracting solution in a high-pressure reverse osmosis or electrodialysis mode, and the high-concentration extracting solution returns to the forward osmosis membrane (1) for continuous use.
8. The method for concentrating an organic solvent according to claim 7, wherein the high pressure reverse osmosis in step b) is performed by introducing a low concentration of the extract into one side of the reverse osmosis membrane (2), increasing the pressure to discharge water molecules in the low concentration of the extract through the other side of the reverse osmosis membrane (2), so that the extract becomes high concentration, and the high concentration of the extract is continuously introduced into the forward osmosis membrane (1).
9. The method for concentrating an organic solvent according to claim 7, wherein the forward osmosis membrane(1) Concentrating 5% DMF organic solvent in 1M NaCl solution as extractive solution, and allowing forward osmosis membrane to have water flux of 1-10L/M2Hr, reverse salt flux 0.1-5g/m2Per hr, the retention rate of the organic solvent is more than 80%.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2014039915A (en) * | 2012-08-23 | 2014-03-06 | Mitsubishi Chemicals Corp | Forward osmosis membrane |
| CN105800851A (en) * | 2016-05-23 | 2016-07-27 | 海博伦（苏州）环境科技股份有限公司 | Forward osmosis drawing solution and cyclic regeneration method and application thereof |
| CN212492418U (en) * | 2020-05-06 | 2021-02-09 | 昕恩希(浙江)科技有限公司 | System for concentrating organic solvents |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2014039915A (en) * | 2012-08-23 | 2014-03-06 | Mitsubishi Chemicals Corp | Forward osmosis membrane |
| CN105800851A (en) * | 2016-05-23 | 2016-07-27 | 海博伦（苏州）环境科技股份有限公司 | Forward osmosis drawing solution and cyclic regeneration method and application thereof |
| CN212492418U (en) * | 2020-05-06 | 2021-02-09 | 昕恩希(浙江)科技有限公司 | System for concentrating organic solvents |
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