CN111167317A - Preparation of high-hydrophobicity hollow fiber membrane and desulfurization wastewater treatment method thereof - Google Patents
Preparation of high-hydrophobicity hollow fiber membrane and desulfurization wastewater treatment method thereof Download PDFInfo
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- CN111167317A CN111167317A CN202010040214.7A CN202010040214A CN111167317A CN 111167317 A CN111167317 A CN 111167317A CN 202010040214 A CN202010040214 A CN 202010040214A CN 111167317 A CN111167317 A CN 111167317A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
- B01D69/08—Hollow fibre membranes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D67/00—Processes specially adapted for manufacturing semi-permeable membranes for separation processes or apparatus
- B01D67/0002—Organic membrane manufacture
- B01D67/0009—Organic membrane manufacture by phase separation, sol-gel transition, evaporation or solvent quenching
- B01D67/0013—Casting processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D67/00—Processes specially adapted for manufacturing semi-permeable membranes for separation processes or apparatus
- B01D67/0079—Manufacture of membranes comprising organic and inorganic components
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- 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
- C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2325/00—Details relating to properties of membranes
- B01D2325/38—Hydrophobic membranes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Abstract
The invention provides a preparation method of a high-hydrophobicity hollow fiber membrane and application of the membrane in desulfurization wastewater treatment, which comprises the following steps: preparing a high-hydrophobic polymer hollow fiber membrane by adopting a non-solvent phase inversion method; membrane distillation is carried out on the pretreated flue gas desulfurization wastewater by utilizing the hollow fiber membrane, so as to realize salt water separation; the waste heat of the flue gas is utilized to increase the temperature of the desulfurization waste water and increase the water flux in the membrane distillation process. The invention is characterized in that: the high-hydrophobicity hollow fiber membrane with small surface aperture and attached hydrophobic particles is obtained by adjusting the ratio of the extrusion rate of the membrane casting solution to the stretching rate of the nascent membrane in the spinning process of the hollow fiber membrane, the prepared hollow fiber membrane is used for carrying out membrane distillation desalination on flue gas desulfurization wastewater, the membrane distillation efficiency is improved by using the waste heat of the flue gas, the special surface property of the membrane material is used for slowing down the rate of salt crystallization on the membrane surface and membrane pollution, and a novel method with high efficiency, energy conservation and environmental protection is provided for the desalination of the desulfurization wastewater.
Description
Technical Field
The invention relates to a preparation of a hollow fiber membrane and a flue gas desulfurization wastewater treatment technology of a thermal power plant, in particular to a method for preparing a high-hydrophobicity hollow fiber membrane by using a non-solvent phase inversion method, desalting desulfurization wastewater by membrane distillation and improving the membrane distillation efficiency by using flue gas waste heat.
Background
Due to the combustion of coal, flue gas containing a large amount of sulfur oxides is generated in the thermal power generation process, and it is necessary to perform desulfurization treatment. A common method of flue gas desulfurization is to wash the flue gas in a reaction tower using a slurry of limestone, lime, or the like, but this desulfurization process generates large waste water. Flue gas desulfurization wastewater is the main sewage source of the current thermal power plant, and has large salt content, strong corrosivity and great harm to the environment. The treatment capacity and cost of the desulfurization wastewater directly influence the operation and the profit of the thermal power plant. At present, the conventional process of domestic flue gas desulfurization wastewater is generally to use chemical or physical flocculation sedimentation and then reuse or discharge after PH regulation. The process can remove suspended matters and most heavy metals, but can not remove sulfate and chloride ions, and trace heavy metals are remained in the treated water. Therefore, the treatment of flue gas desulfurization wastewater by conventional processes does not meet the requirement of zero emission.
Zero emission refers to the activity of infinitely reducing pollutant and energy emission to zero, namely zero emission not only minimizes the energy consumption in the implementation process, but also minimizes the amount of pollutants which need to be discharged finally, and finally eliminates non-renewable resources and energy. The zero discharge of the flue gas desulfurization wastewater refers to a process of concentrating the desulfurization wastewater by an energy-saving and environment-friendly method and completely recycling finally obtained salts and pure water. At present, the flue gas desulfurization waste water zero discharge technology mainly comprises flue gas evaporation, forced circulation of a crystal seed method and a softening-concentration-forced crystallization process, but the methods have the disadvantages. The flue gas evaporation is that the desulfurization wastewater is atomized firstly and then evaporated in the flue by high temperature in the flue, and the method requires high flue gas temperature and low practical applicability. The forced circulation of the seed crystal method is to add seed crystals in the evaporation process and realize the separation of salt and water through the crystallization of salt. The method has the defects of high energy consumption, easy scaling of the system and unstable operation. The softening-concentrating-forced crystallization process consumes a large amount of chemical agents and generates a large amount of sludge, which not only causes secondary pollution, but also has high cost.
The membrane separation method is a new important method for treating industrial wastewater, and the operation process does not need to use a large amount of chemical agents, and has the advantages of easy installation of equipment, small occupied area, environmental protection, high efficiency and the like. Most of the current industrial water desalination is based on reverse osmosis membrane separation. The membrane separation method based on reverse osmosis has high desalination efficiency, but higher transmembrane pressure is required to be applied to two sides of the membrane to overcome the osmotic pressure of the high-salinity wastewater, the process has high energy consumption and large loss to equipment, and the long-term stable operation of the equipment is not facilitated. The design of the desulfurization wastewater zero-discharge treatment system with low energy consumption and environmental protection by combining the characteristics of the flue gas of the thermal power plant and the desulfurization wastewater has important significance.
The membrane distillation desalination is a novel separation method which takes temperature difference as power and drives purified water to transfer mass in a membrane material, and the larger the temperature difference at two sides of a membrane wall is, the faster the mass transfer rate of the purified water in the membrane is. Compared with the traditional reverse osmosis desalination which takes pressure as the driving force of mass transfer, the membrane distillation is particularly suitable for the desalination of water bodies which can utilize waste heat. The membrane distillation process has the other characteristic that the mass transfer of water in the membrane material is carried out by the diffusion and condensation of water vapor, and the mass transfer of liquid is avoided to the maximum extent, so that the high desalination efficiency (> 99.9%) of the membrane distillation is ensured. Therefore, the hollow fiber membrane used for membrane distillation should have high hydrophobicity to reduce unnecessary membrane wetting, but the hydrophobicity of the polymer hollow fiber membrane prepared by a single polymer through a phase inversion method is limited. The hydrophobic property of the membrane material can be further improved by depositing hydrophobic nano particles on the inner surface of the hollow fiber membrane.
Another important problem faced by membrane distillation is membrane wetting, membrane fouling and consequent reduction in water flux and desalination efficiency caused by salt precipitation on the inner surface of the membrane. The precipitation of salts on the inner surface of the membrane is a gradually developing process, and the first step is that partial salt-containing solution permeates into the inner surface of the membrane to cause large-area infiltration of the membrane, so that crystal nuclei are formed on the surface of the membrane and the precipitation of the salts is accelerated. The hydrophobic hollow fiber membrane with high surface hydrophobicity, small aperture and loose middle layer structure can slow down the rate of salt precipitation on the inner surface of the membrane.
Disclosure of Invention
The patent discloses a preparation method of a high-hydrophobicity hollow fiber membrane and application thereof in desulfurization wastewater treatment, which comprises the following steps: obtaining a hollow fiber membrane with small inner surface aperture and hydrophobic particle adhesion by adjusting the ratio of the extrusion rate of the membrane casting solution to the stretching rate of the nascent membrane in the preparation process of the hollow fiber membrane; the prepared membrane material is packaged into a hollow fiber membrane component for membrane distillation of flue gas desulfurization wastewater, and flue gas waste heat is utilized to improve the membrane distillation efficiency. The invention prepares the modified membrane material with a special structure, and the modified membrane material is used for membrane distillation of the desulfurization wastewater, thereby reducing the pollution speed of the membrane material and improving the efficiency of the membrane distillation. In a preferred implementation, the method comprises the steps of:
preparing a polymer hollow fiber membrane by adopting a solution phase inversion method, wherein in the process, the used hollow fiber membrane casting solution contains hydrophobic modified nano particles, and the ratio of the extrusion rate of the casting solution to the stretching rate of a primary membrane is (2): 30 to 2: 50, the prepared hollow fiber membrane has obvious polymer stretching orientation on the inner surface and is attached with hydrophobic nano particles.
And packaging the dried hollow fiber membrane into a membrane component with a certain effective area by using an epoxy resin adhesive, wherein the membrane component is provided with two independent channels, the inner channel of the membrane component is an inner cavity of the hollow fiber membrane, and the outer channel of the membrane component is a channel between the outer surface of the hollow fiber membrane and the shell of the membrane component.
The storage tank filled with the pretreated flue gas desulfurization wastewater, the circulating pump, the hollow fiber membrane module and the cooling water bath are connected with a membrane distillation system through pipelines. Flue gas desulfurization waste water is introduced into an inner channel of the hollow fiber membrane module, and cooling water is introduced into an outer channel of the hollow fiber membrane module. And leading the desulfurization waste water flowing out from the inner outlet of the hollow fiber membrane component into the desulfurization waste water storage tank again after passing through the crystallization device.
The desulfurization waste water circulation pipeline in the membrane distillation system is arranged in the flue gas circulation pipeline, and a certain space is formed between the desulfurization waste water circulation pipeline and the flue gas circulation pipeline.
The high temperature flue gas is directed to a flue gas flow duct and ultimately to a desulfurization tower.
The temperature of purified water in the external channel of the membrane module is reduced by using a cooling water bath, and the temperature of desulfurization wastewater in the internal channel of the hot membrane module is increased by using waste heat of flue gas, so that fluids on two sides of the hollow fiber membrane have proper temperature difference.
And circulating fluid in the inner channel and the outer channel of the membrane module by using a power pump, and transferring the purified water from the inner channel of the membrane module to the outer channel of the membrane module by taking the temperature difference of the two sides of the membrane as driving force. The purified water penetrating through the membrane is collected in a purified water storage tank, and the concentrated desulfurization wastewater is continuously circulated in the inner channel of the membrane component after passing through the crystallization unit.
A clean water storage tank connected to the external channels of the membrane module will collect the clean water that has permeated the membrane and the collected clean water can be used for further desulfurization of the flue gas. The salt collected in the crystallization unit is periodically transported out.
Drawings
FIG. 1: section electron microscope photograph of hollow fiber membrane
FIG. 2: electron microscope photograph of inner surface of hollow fiber membrane
FIG. 3: electron microscope photograph of outer surface of hollow fiber membrane
FIG. 4: a schematic diagram of a desulfurization wastewater membrane distillation desalination process based on flue gas waste heat. Wherein 1-a flue gas desulfurization tower; 2-desulfurization waste water storage tank; 3-desulfurization waste water circulating pump; 4-flue gas inlet; 5, a desulfurization wastewater circulating pipeline; 6-flue gas flow ducts; 7-a crystallization device; 8-hollow fiber membrane module; 9-clean water circulation pipeline; 10-a purified water storage tank; 11-a water purification circulating pump; 12-cooling water bath. 13, 14-external channel branch port of membrane module
Detailed Description
The technical scheme of the invention is further explained by the specific implementation mode in combination with the attached drawings. It is to be understood that the specific embodiments described herein are merely illustrative of the invention and are not limiting of the invention. It should be further noted that, for the convenience of description, only some but not all of the relevant aspects of the present invention are shown in the drawings.
Example 1
And (3) preparing a hollow fiber membrane.
N-methyl pyrrolidone (NMP) or dimethyl acetamide (DMAC) is used as a solvent to prepare the nano-composite material containing 20 wt% of PVDF, 5 wt% of pore-forming agent and 1.5 wt% of hydrophobic modified nano-TiO2Sol casting solution, and vacuum defoaming the prepared solution. Extruding the casting solution from a hollow fiber membrane spinning head by a metering pump at a certain linear velocity, feeding the primary membrane into an external flocculation tank after the primary membrane undergoes an air bath stroke with the length of 5-10cm, and winding the primary membrane by a winding device at a certain linear velocity. The ratio of the extrusion speed of the casting solution to the stretching speed of the primary film is 2: 30 to 2: between 50.
Characterization of hollow fiber membranes.
And soaking the prepared hollow fiber membrane in tap water at room temperature for two days, and then carrying out solvent exchange and drying to obtain the high-hydrophobicity hollow fiber membrane. And (3) brittle-breaking the dried hollow fiber membrane in liquid nitrogen to obtain a cross section characterization sample. And wrapping the dried hollow fiber membrane bundle with epoxy resin, and after the epoxy resin is completely cured, performing 60-degree beveling on the membrane bundle to expose the inner surface of the membrane in the air to obtain an inner surface characterization sample. And spraying gold on the outer surface, the cross section and the inner surface of the dried hollow fiber membrane, and observing the micro appearance of the hollow fiber membrane by using a scanning electron microscope. As can be seen from fig. 1, the prepared hollow fiber membrane has obvious finger-shaped pores near the inner and outer layers, and the intermediate layer has a typical sponge shape, which indicates that the phase inversion speed of the inner and outer surfaces is faster during the preparation process of the hollow fiber membrane, and also means that the pore diameters of the inner and outer surfaces of the hollow fiber membrane are smaller (see fig. 2 and fig. 3); in addition, the inner surface of the membrane shows a significant pore morphology orientation due to a stretching effect during membrane spinning, and the hydrophobic nanoparticles in the dope solution are concentrated on the inner surface of the hollow fiber membrane (see fig. 2).
Membrane distillation of desulfurized waste water based on highly hydrophobic hollow fiber membranes.
The prepared hollow fiber membrane is encapsulated by epoxy resin to prepare a hollow fiber membrane component with a certain effective area for membrane distillation of desulfurization wastewater. The disclosed membrane distillation system based on highly hydrophobic hollow fiber membrane comprises the following parts (see fig. 4): the device comprises a desulfurizing tower 1, a desulfurizing waste water storage tank 2, a desulfurizing waste water circulating pump 3, a flue gas inlet 4, a desulfurizing waste water circulating pipeline 5, a flue gas circulating pipeline 6, a salt crystallization device 7, a hollow fiber membrane module 8, a purified water circulating pipeline 9, a purified water storage tank 10, a purified water circulating pump 11, a cooling water bath 12 and membrane module external channel branch ports 13 and 14. Wherein the purified water storage tank 10 is connected with a purified water circulating pump 11, a cooling water bath 12 and external channel branch ports 13 and 14 of the membrane module 8 in sequence, and is guided back to the purified water storage tank 10 through a purified water circulating pipeline 9 for circulating and cooling purified water in an external channel of the membrane module 8; the desulfurization waste water storage tank 2 is sequentially connected with a desulfurization waste water power pump 3, a desulfurization waste water circulation pipeline 5, an internal channel of a membrane component 8 and a crystallization device 7, and is guided back to the desulfurization waste water storage tank 2 through the desulfurization waste water circulation pipeline 5; the downstream of the desulfurization waste water circulating pipeline 5 is connected with the inlet at the lower end of the internal channel of the membrane component 8, the crystallizing device 7 and the flue gas circulating pipeline 6 in sequence and is guided back to the flue gas desulfurization tower 1 for circularly heating the desulfurization waste water.
The high temperature flue gas is introduced into a flue gas flow duct 6, and a waste water flow duct 5 is partially disposed inside the flue gas flow duct 6 to heat the desulfurization waste water duct 5 by waste heat.
The desulfurization waste water discharged from the desulfurization tower 1 enters a desulfurization waste water storage tank 2 after being pretreated. The pretreatment of the desulfurization wastewater may include: washing the flue gas by using an alkaline aqueous solution containing calcium ions; a portion of the insoluble compounds and suspended organics are removed by settling, or ultrafiltration. After entering the storage tank 2, the pretreated desulfurization wastewater is introduced into the internal passage of the hollow fiber membrane module 8 from the lower end of the hollow fiber membrane module 8 by the circulating pump, and is returned to the storage tank 2 after passing through the crystallization device 7.
The high-temperature desulfurization waste water and the cooling water undergo membrane distillation in the hollow fiber membrane module 8, the purified water is transferred from the desulfurization waste water in the internal passage of the membrane module 8 to the cooling water in the external passage of the membrane module 8, and the transferred purified water is brought into the purified water storage tank 10 by the purified water circulation pump 11. Wherein the temperature of the desulfurization wastewater is 60-70 ℃; the flow speed of the desulfurization waste water is set to be 170-250m/min, the flow speed of the cooling water is set to be 6-10m/min, and the desalting efficiency of more than 99.9 percent and higher pure water flux can be obtained.
A crystallizing device 7 placed in the cold side water circulation path crystallizes and retains a part of the salt therein. The solid salt retained in the crystallization apparatus is periodically transported outside.
The present invention is not limited to the above preferred embodiments, and any modifications, equivalent replacements, improvements, etc. within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (9)
1. A preparation method of a high-hydrophobicity hollow fiber membrane and a desulfurization wastewater treatment method thereof are characterized in that: preparing a hollow fiber membrane with hydrophobic particles attached to the surface by a solution phase inversion method, and packaging the prepared hollow fiber membrane into a hollow fiber membrane component; circulating the pretreated flue gas desulfurization wastewater in an internal channel of the hollow fiber membrane module through a circulating pump, circulating cold water in an external channel of the hollow fiber membrane module, and driving purified water to be transferred from an internal channel to an external channel of the hollow fiber membrane module by taking the temperature difference of two sides of the wall of the hollow fiber membrane as power; and (4) recovering salts in the desulfurization wastewater by using a crystallization device.
2. The method of claim 1, wherein: in the process of preparing the polymer hollow fiber membrane by adopting a non-solvent phase inversion method, the used hollow fiber membrane casting solution contains hydrophobic modified nano particles, and the ratio of the extrusion rate of the casting solution to the stretching rate of the primary membrane is (2): 30 to 2: between 50; the polymer used for preparing the hollow fiber membrane can be polyvinylidene fluoride or polyether sulfone, and the used hydrophobic modified nano particles are hydrophobic titanium dioxide or hydrophobic silicon dioxide.
3. The method of claim 1, wherein: the hollow fiber membrane is a hydrophobic hollow fiber membrane, the aperture of the inner surface is 200-300nm, the aperture of the outer surface is 200-500nm, and the inner surface is attached with hydrophobic modified nano particles.
4. The method of claim 1, wherein: the hollow fiber membrane module is an array consisting of a plurality of hollow fiber membrane module units; the inner channel of the hollow fiber membrane component is the inner cavity of the hollow fiber membrane; the external passage of the hollow fiber membrane module refers to a passage between the outer surface of the hollow fiber membrane and the membrane module housing.
5. The method of claim 1, wherein: after the desulfurization wastewater is pretreated, part of insoluble solids in the desulfurization wastewater are removed; the partial circulation path of the desulfurization waste water is arranged in the flue gas path, and the flue gas raises the temperature of the desulfurization waste water to 60-70 ℃ through a flow pipeline for heating the desulfurization waste water.
6. The method of claim 1, wherein: and reducing the temperature of the purified water in the external channel of the hollow fiber membrane component to 5-10 ℃ by utilizing circulating water bath.
7. The method of claim 1, wherein: the temperature difference between the inner side and the outer side of the hollow fiber membrane is used as power, pure water is transferred from the desulfurization wastewater in the internal channel of the membrane module to the pure water in the external channel of the membrane module, the concentrated saline wastewater continuously participates in circulation, and the rejection rate of the hollow fiber membrane to salt in the desulfurization wastewater is more than 99.9%.
8. The method of claim 1, wherein: a crystallization unit is arranged in a flow path of the desulfurization wastewater to be treated, and salts in the desulfurization wastewater are recovered; the crystallization unit is an evaporation crystallization device.
9. The method of claim 1, wherein: the purified water circulated in the external passage of the hollow fiber membrane module is tap water or equipment cooling water, specifically, machine furnace cooling water and bearing cooling water.
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| CN202010040214.7A CN111167317A (en) | 2020-01-15 | 2020-01-15 | Preparation of high-hydrophobicity hollow fiber membrane and desulfurization wastewater treatment method thereof |
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| CN202010040214.7A CN111167317A (en) | 2020-01-15 | 2020-01-15 | Preparation of high-hydrophobicity hollow fiber membrane and desulfurization wastewater treatment method thereof |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114225589A (en) * | 2021-12-15 | 2022-03-25 | 东莞理工学院 | Pollutant removal, moisture and waste heat recovery integrated device and method based on hydrophilic hollow fiber membrane |
| US11548784B1 (en) | 2021-10-26 | 2023-01-10 | Saudi Arabian Oil Company | Treating sulfur dioxide containing stream by acid aqueous absorption |
| US11596899B1 (en) | 2021-12-20 | 2023-03-07 | Saudi Arabian Oil Company | Hollow fiber membrane module and method of making and using same |
| US11926799B2 (en) | 2021-12-14 | 2024-03-12 | Saudi Arabian Oil Company | 2-iso-alkyl-2-(4-hydroxyphenyl)propane derivatives used as emulsion breakers for crude oil |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101121639A (en) * | 2007-07-13 | 2008-02-13 | 天津大学 | Membrane distillation dehydration method for polyatomic alcohol water solution produced from corn |
| CN102114390A (en) * | 2009-12-30 | 2011-07-06 | 中国科学院生态环境研究中心 | Reinforced type polyvinylidene fluoride hollow fiber hydrophobic membrane and preparation method thereof |
| CN102234144A (en) * | 2010-05-05 | 2011-11-09 | 天津工业大学 | Membrane distillation water purifying device and method |
| CN103373786A (en) * | 2012-04-28 | 2013-10-30 | 北京林业大学 | Method for treating reverse osmosis concentrate |
| CN104548950A (en) * | 2013-10-16 | 2015-04-29 | 中国石油化工股份有限公司 | Inorganic nanoparticle enhanced type polypropylene hollow fiber microporous membrane and preparation method thereof |
| CN107899435A (en) * | 2017-11-17 | 2018-04-13 | 博天环境集团股份有限公司 | A kind of preparation method of polyvinylidene fluoride dewatering hollow-fibre membrane |
| CN108726770A (en) * | 2017-04-24 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of advanced treatment and reclamation method of flue gas desulfurization liquid |
| CN110180403A (en) * | 2019-04-30 | 2019-08-30 | 浙江汉青环境科技有限公司 | A kind of fiber tube enhancement type doughnut composite biological film and preparation method and application |
-
2020
- 2020-01-15 CN CN202010040214.7A patent/CN111167317A/en not_active Withdrawn
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101121639A (en) * | 2007-07-13 | 2008-02-13 | 天津大学 | Membrane distillation dehydration method for polyatomic alcohol water solution produced from corn |
| CN102114390A (en) * | 2009-12-30 | 2011-07-06 | 中国科学院生态环境研究中心 | Reinforced type polyvinylidene fluoride hollow fiber hydrophobic membrane and preparation method thereof |
| CN102234144A (en) * | 2010-05-05 | 2011-11-09 | 天津工业大学 | Membrane distillation water purifying device and method |
| CN103373786A (en) * | 2012-04-28 | 2013-10-30 | 北京林业大学 | Method for treating reverse osmosis concentrate |
| CN104548950A (en) * | 2013-10-16 | 2015-04-29 | 中国石油化工股份有限公司 | Inorganic nanoparticle enhanced type polypropylene hollow fiber microporous membrane and preparation method thereof |
| CN108726770A (en) * | 2017-04-24 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of advanced treatment and reclamation method of flue gas desulfurization liquid |
| CN107899435A (en) * | 2017-11-17 | 2018-04-13 | 博天环境集团股份有限公司 | A kind of preparation method of polyvinylidene fluoride dewatering hollow-fibre membrane |
| CN110180403A (en) * | 2019-04-30 | 2019-08-30 | 浙江汉青环境科技有限公司 | A kind of fiber tube enhancement type doughnut composite biological film and preparation method and application |
Non-Patent Citations (1)
| Title |
|---|
| 吴智华主编: "《高分子材料加工工程实验教程》", 30 September 2004, 化学工业出版社 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11548784B1 (en) | 2021-10-26 | 2023-01-10 | Saudi Arabian Oil Company | Treating sulfur dioxide containing stream by acid aqueous absorption |
| US11926799B2 (en) | 2021-12-14 | 2024-03-12 | Saudi Arabian Oil Company | 2-iso-alkyl-2-(4-hydroxyphenyl)propane derivatives used as emulsion breakers for crude oil |
| CN114225589A (en) * | 2021-12-15 | 2022-03-25 | 东莞理工学院 | Pollutant removal, moisture and waste heat recovery integrated device and method based on hydrophilic hollow fiber membrane |
| US11596899B1 (en) | 2021-12-20 | 2023-03-07 | Saudi Arabian Oil Company | Hollow fiber membrane module and method of making and using same |
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