CN115367838B - Membrane contactor system for recycling anaerobic effluent dissolved methane - Google Patents
Membrane contactor system for recycling anaerobic effluent dissolved methane Download PDFInfo
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 110
- 239000012528 membrane Substances 0.000 title claims abstract description 92
- 238000004064 recycling Methods 0.000 title abstract description 11
- 239000007788 liquid Substances 0.000 claims abstract description 65
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 42
- 230000010412 perfusion Effects 0.000 claims abstract description 29
- 239000007789 gas Substances 0.000 claims abstract description 22
- 239000012159 carrier gas Substances 0.000 claims abstract description 17
- 238000011049 filling Methods 0.000 claims abstract description 13
- 230000002572 peristaltic effect Effects 0.000 claims abstract description 8
- 238000003860 storage Methods 0.000 claims abstract description 7
- 239000000126 substance Substances 0.000 claims abstract description 5
- 239000002351 wastewater Substances 0.000 claims description 23
- 239000002033 PVDF binder Substances 0.000 claims description 9
- 229920002981 polyvinylidene fluoride Polymers 0.000 claims description 9
- 239000003978 infusion fluid Substances 0.000 claims description 5
- 239000011148 porous material Substances 0.000 claims description 4
- 238000001802 infusion Methods 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- 239000000741 silica gel Substances 0.000 claims description 2
- 229910002027 silica gel Inorganic materials 0.000 claims description 2
- -1 polytetrafluoroethylene Polymers 0.000 claims 2
- 230000037452 priming Effects 0.000 claims 2
- 239000004205 dimethyl polysiloxane Substances 0.000 claims 1
- 229920001600 hydrophobic polymer Polymers 0.000 claims 1
- 229920000435 poly(dimethylsiloxane) Polymers 0.000 claims 1
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims 1
- 239000004810 polytetrafluoroethylene Substances 0.000 claims 1
- 238000012546 transfer Methods 0.000 abstract description 8
- 238000011084 recovery Methods 0.000 abstract description 6
- 239000003463 adsorbent Substances 0.000 abstract description 2
- 238000003889 chemical engineering Methods 0.000 abstract description 2
- 238000007872 degassing Methods 0.000 abstract description 2
- 238000011161 development Methods 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000004065 wastewater treatment Methods 0.000 abstract description 2
- 230000007774 longterm Effects 0.000 abstract 1
- 239000012071 phase Substances 0.000 description 10
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 6
- 230000004907 flux Effects 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- 230000005501 phase interface Effects 0.000 description 4
- 238000009987 spinning Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 238000001291 vacuum drying Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000010041 electrostatic spinning Methods 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 230000002209 hydrophobic effect Effects 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 239000012466 permeate Substances 0.000 description 2
- 230000002000 scavenging effect Effects 0.000 description 2
- 229920002545 silicone oil Polymers 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000013519 translation Methods 0.000 description 2
- 208000005156 Dehydration Diseases 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002121 nanofiber Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000013557 residual solvent Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 229910021642 ultra pure water Inorganic materials 0.000 description 1
- 239000012498 ultrapure water Substances 0.000 description 1
- 238000005303 weighing Methods 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- 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
-
- 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
- B01D67/0081—After-treatment of organic or inorganic membranes
- B01D67/0088—Physical treatment with compounds, e.g. swelling, coating or impregnation
-
- 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
- B01D67/0081—After-treatment of organic or inorganic membranes
- B01D67/0095—Drying
-
- 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
- B01D69/02—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor characterised by their properties
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/30—Polyalkenyl halides
- B01D71/32—Polyalkenyl halides containing fluorine atoms
- B01D71/34—Polyvinylidene fluoride
-
- 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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2323/00—Details relating to membrane preparation
- B01D2323/39—Electrospinning
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Manufacturing & Machinery (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Degasification And Air Bubble Elimination (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a novel membrane contactor system for recycling anaerobic effluent dissolved methane, belonging to the technical fields of wastewater treatment, chemical engineering and environmental protection. The device comprises a water inlet tank, a peristaltic pump, an air pump, a buffer container, a liquid filling membrane contactor module, an air storage tank, a pressure gauge, a flowmeter and the like, wherein the liquid filling membrane contactor module mainly comprises a two-sided clamping device and a liquid filling membrane, and a cavity channel on two sides is formed by isolating grooves of the clamping device through the membrane, so that water flow and air flow respectively flow reversely on two sides of the liquid filling membrane. The system can fully utilize the gas partial pressure difference and chemical potential difference of three phases of anaerobic effluent, perfusion liquid film and carrier gas and the difference of intermolecular acting force (such as solubility) of the perfusion liquid and methane molecules or water molecules to selectively drive methane mass transfer, so that the recovery efficiency and purity of dissolved methane are obviously improved, the use of a large amount of adsorbents and secondary degassing treatment are not involved, the system is environment-friendly and low in cost, and has important practical significance and long-term strategic significance for improving the recycling and sustainable development capacity of anaerobic biological treatment.
Description
Technical Field
The invention belongs to the technical fields of wastewater treatment, chemical engineering and environmental protection, and relates to a resource recovery system for treating dissolved methane in anaerobic wastewater based on a liquid perfusion membrane contactor.
Background
Anaerobic biotechnology, which can convert wastewater into clean water and methane energy, is widely used in sewage treatment plants in various regions of the world, and has become an important means for alleviating global water crisis and energy shortage. Nevertheless, due to the advection limitation of anaerobic reactor (such as Upflow Anaerobic Sludge Blanket (UASB)) systems, the generated methane accounts for about 11-100% and is discharged to the environment along with anaerobic effluent in a dissolved state, so that not only a great deal of energy loss is caused, but also secondary problems such as greenhouse effect (the greenhouse effect is 25 times of carbon dioxide), explosion (the explosion limit is 1.4 mg/L) and the like are caused, and the efficient recycling and sustainable development of anaerobic biotechnology are severely restricted. Thus, recovery of dissolved methane in anaerobic effluent is of great practical importance.
Currently, techniques available for separating dissolved methane from anaerobic effluent include stripping, spray aeration, packed columns, membrane contactors, and the like. However, the operation problems such as water bubbles or flooding are extremely easy to occur in the stripping, spray aeration and packed towers which conduct methane mass transfer through the direct contact of anaerobic wastewater and carrier gas. The membrane contactor takes a hydrophobic membrane as a barrier for isolating a gas phase from a liquid phase, is driven by a gas partial pressure difference provided by vacuum or scavenging, and methane is firstly transferred from an anaerobic wastewater body to a wastewater/membrane phase interface, then enters the membrane phase and is diffused and transferred to the membrane phase/gas phase interface, and finally reaches the gas phase body, so that the methane is effectively recovered. Therefore, the gas and liquid operation parameters of the membrane contactor are independently controllable, the problems can be effectively avoided, and the membrane contactor also has the advantages of large specific surface area per unit volume, low energy consumption, small occupied area and the like, and has great potential in the aspect of recovering anaerobic effluent to dissolve methane. However, the methane recovery process of the membrane contactor not only involves gas-liquid (liquid water/methane) separation, but also changes part of anaerobic effluent from liquid to gas (water vapor) under the drive of vacuum or scavenging, while the wastewater/membrane phase interface of the traditional membrane contactor has lower selectivity to methane and water vapor, and the process of recovering anaerobic effluent to dissolve methane is usually accompanied by high water vapor flux, which accelerates condensation of water vapor in the membrane, reduces mass transfer flux of methane, and causes the recovered mixed gas to contain a large amount of water vapor, so that low-concentration methane needs to be separated from the generated gas mixture before recycling, and even if heat and power co-production is performed, energy intensive secondary dehydration treatment is also required.
Disclosure of Invention
The invention aims to solve the problems of low recovery efficiency, low selectivity and the like in the process of recovering anaerobic effluent dissolved methane by a traditional membrane contactor system, adopts a novel membrane contactor system for recovering anaerobic effluent dissolved methane, can fully utilize the gas partial pressure difference and chemical potential difference of three phases of anaerobic effluent, a perfusion liquid membrane and carrier gas, and the difference of intermolecular acting forces (such as solubility) between the perfusion liquid and methane molecules or water molecules, selectively drives methane mass transfer, and is different from the traditional membrane contactor system (figure 2) in the mass transfer process, and the methane molecule transfer step: (1) Methane molecules are transferred from the wastewater phase to the wastewater phase/liquid perfusion membrane interface; (2) Methane molecules are bound-solvated (water molecules are trapped) with the perfusion liquid by intermolecular forces at the interface; (3) Methane molecules enter the liquid perfusion membrane and are transferred to the liquid perfusion membrane/carrier gas phase interface; (4) The methane molecules desorb at the interface and transfer to the carrier gas phase body. The system can remarkably improve the recovery efficiency and purity of dissolved methane, does not involve the use of a large amount of adsorbents and secondary degassing treatment, is environment-friendly and low in cost, and has important significance in ensuring public safety, reducing greenhouse effect and optimizing energy structures.
For this purpose, the technical scheme of the invention is as follows:
a novel membrane contactor system (figure 1) for recycling anaerobic effluent dissolved methane comprises a water inlet tank, a peristaltic pump, an air pump, a buffer container, a membrane contactor module, an air storage tank, a pressure gauge, a flowmeter and the like; the membrane contactor module mainly comprises two clamping devices and a liquid filling membrane; the middle part of the inner side of the clamping device is a cubic groove, and the outer side of the clamping device is respectively provided with two threaded round holes communicated with two ends of the groove, and the two threaded round holes are externally connected with a quick plug to serve as a water (air) inlet and a water (air) outlet; the liquid infusion membrane comprises a porous base membrane and an infusion liquid, the infusion liquid being confined within the porous base membrane; the poly (micro) Kong Jimo has a high porosity; the perfusion liquid is a liquid with high methane solubility, low water solubility (water-immiscible), low volatility, affinity with the base film and affinity greater than water; the liquid filling film is fixed between the two clamping devices through the screws and the silica gel gaskets, and the liquid filling film and the inner walls of the grooves of the clamping devices on the two sides can respectively form an anaerobic wastewater channel and a carrier gas channel. The anaerobic wastewater to be treated is pumped into a buffer container through a peristaltic pump, then enters a wastewater channel of a liquid perfusion membrane contactor for treatment at relatively stable flow and pressure, meanwhile, air is pumped into a carrier gas channel of the liquid perfusion membrane contactor through an air pump in the opposite direction to water flow, the pressure and flow of inlet water and outlet water and inlet and outlet air are monitored through a pressure gauge and a flowmeter, finally, dissolved methane in the wastewater is driven by the chemical potential difference provided by perfusion liquid and the gas partial pressure difference provided by carrier gas together to permeate through a liquid perfusion diffusion membrane to reach a gas phase (carrier gas channel), and is collected by a gas storage tank, and the circulation of water molecules is blocked.
Preferably: the porous base film is a polyvinylidene fluoride fiber film; the pore diameter of the porous base membrane is 0.1-0.2 mu m; the porosity of the porous base film is 80% -90%.
Preferably: the perfusion liquid is silicone oil with the viscosity of 20-500 cts.
Preferably: the liquid infusion membrane is formed by combining a porous base membrane with an infusion liquid by a spin coater with a rotation speed of 2000rpm-4000rpm.
Preferably: the system operates at a transmembrane pressure of 5-50kpa.
Preferably: the gas-liquid ratio of the operation of the system is 0.5-1.
Drawings
FIG. 1 is a schematic diagram of a novel membrane contactor system for recovering anaerobic effluent dissolved methane according to the present invention.
Fig. 2 is a schematic diagram of a conventional membrane contactor and a liquid-filled membrane contactor module.
Fig. 3 is a graph comparing methane and water vapor flux for a conventional membrane contactor and a liquid perfused membrane contactor.
Fig. 4 is a physical diagram of a conventional membrane contactor module at different stages of operation of the liquid-perfused membrane contactor module.
The specific embodiment is as follows:
the technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings, and it is obvious that the described embodiments are some, but not all embodiments of the present invention, and in no way limit the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
A novel membrane contactor system for recycling anaerobic effluent dissolved-state methane comprises a water inlet tank 1, a peristaltic pump 2, an air pump 3, a buffer container 4, a membrane contactor module 7, an air storage tank 8, a pressure gauge 9, a flowmeter 10 and the like, wherein the membrane contactor module mainly comprises a clamping device 6 and a liquid perfusion membrane 12. Anaerobic effluent to be treated in the water inlet tank 1 is pumped into the buffer container 4 through the peristaltic pump 2 and then enters the waste water channel of the liquid filling membrane contactor module 7 for treatment at relatively stable flow and pressure, meanwhile, air is pumped into the carrier gas channel of the liquid filling membrane contactor 7 in the direction opposite to water flow through the air pump 3, the pressure and flow of the water inlet and outlet and the pressure and flow of the air inlet and outlet are monitored through the pressure gauge 9 and the flow meter 10, and finally, dissolved methane in the waste water permeates through the liquid filling membrane 12 to reach gas phase (carrier gas channel) under the common driving of chemical potential difference provided by filling liquid and gas partial pressure difference provided by carrier gas, and is collected by the gas storage tank 8.
Example 1
The method for treating the anaerobic wastewater containing dissolved methane by using the liquid perfusion membrane contactor system with the recycling function comprises the following steps of:
the treated object is artificially synthesized dissolved methane wastewater, and the preparation method comprises the following steps:
injecting 16L of ultrapure water into a 20L water distribution tank, opening methane gas inlet, adjusting the gas inlet pressure to 1bar, adjusting the gas inlet pressure to 2bar, and keeping 50cm 3/ Introducing methane gas at the speed of min until the pressure in the tank body is stabilized to 2bar, closing the air inlet, starting a constant-temperature magnetic stirrer, setting a constant temperature of 25 ℃, rotating a rotor at the temperature of 25 ℃ to 2000rpm, and stirring for 12h to prepare the synthetic wastewater with the dissolved methane concentration of 25+/-5 mg/L.
The method for preparing the liquid perfusion membrane comprises the following steps:
weighing polyvinylidene fluoride (PVDF) powder with certain mass, and placing the powder in a vacuum drying oven at 80 ℃ for drying for more than 4 hours. The dried PVDF powder is weighed and dissolved in Dimethylformamide (DMF) solvent to prepare a mixed solution with 15wt percent, and then the mixed solution is continuously stirred for 12 hours at 45 ℃ to obtain uniform and stable spinning solution. And (3) standing and defoaming for a certain time in a vacuum drying box until no bubbles appear. Setting spinning technological parameters: the jet flow rate is 0.2mm/min; a positive voltage of 13V; a negative voltage of 2V; humidity 40%; a temperature of 30; a receiving distance of 15cm at DEG C; receiving the rotating speed of the rotary drum to be 100rpm; a translation distance of about 10mm; the translation speed is 150mm/min; and starting the electrostatic spinning machine, and spinning for 10 hours. And after spinning the film, taking down the spun PVDF electrostatic spinning nanofiber hydrophobic film, putting the film into a vacuum drying oven at 30 ℃ for drying for more than 0.5h so as to facilitate volatilization of residual solvent or moisture, and finally, pressing and flattening the film by using a glass plate. Cutting the porous membrane into proper size, fixing on a disc of a spin coater, regulating the rotation speed to 4000rpm, selecting silicon oil which has higher methane solubility than water, lower volatility, is insoluble with water, has affinity with PVDF membrane and has affinity larger than water as pouring liquid, pouring into the spin coater, closing the spin coater after 1min, and taking out the liquid pouring membrane.
Constructing a novel liquid perfusion membrane contactor module:
the porous PVDF fiber membrane and the liquid perfusion membrane (silicone oil perfused porous PVDF membrane) are respectively sealed in a gas-liquid separation cavity through a clamping device, and a traditional membrane contactor module and a novel liquid perfusion membrane contactor module are constructed, wherein the membrane and the inner walls of grooves of the clamping devices on two sides form an anaerobic wastewater channel and a carrier gas channel. The contactor module is connected to the system in the vertical direction, the separation process does not depend on the action of gravity, the system is started in a circulating convection operation mode (schematic diagram 1), the synthetic wastewater is stably pumped into the gas-liquid membrane contactor at the flow rate of 5L/h through the peristaltic pump and the buffer container, so that the synthetic wastewater circularly flows on one side of the membrane, and nitrogen on the other side is circulated at the flow rate of 60 cm 3 The flow rate/min was used as a purge gas to the membrane with a gas-liquid ratio of about 0.72 and a transmembrane pressure difference of 20Kpa.
As shown in FIG. 3, the methane mass transfer flux of the liquid-filled membrane contactor system is 3.435 mol/m 2 Per hour, significantly higher than 0.869mol/m of conventional membrane contactors 2 And/h. Moreover, the liquid-perfused membrane contactor has high water vapor/methane selectivity, water vapor flux of almost 0, and recovered methane of higher purity, compared with porous membrane water vapor flux of 1.233mol/m 2 And/h. In addition, as shown in fig. 4, a significant capillary condensation phenomenon can be found at the air outlet of the conventional membrane contactor in comparison with the liquid-perfused membrane contactor. Therefore, the novel membrane contactor system for recycling anaerobic effluent dissolved methane can remarkably improve the recycling efficiency and purity of the dissolved methane.
Claims (3)
1. A membrane contactor system for recovering anaerobic effluent dissolved methane, characterized in that: the system comprises a water inlet tank, a peristaltic pump, an air pump, a buffer container, a liquid perfusion membrane contactor module, an air storage tank, a pressure gauge and a flowmeter, anaerobic effluent to be treated is pumped into the buffer container through the peristaltic pump, flows into a waste water channel of the liquid perfusion membrane contactor module at a stable flow rate and pressure, meanwhile, air is pumped into a carrier gas channel of the liquid perfusion membrane contactor module through the air pump in a direction opposite to water flow, the pressure and flow rate of the inlet and outlet air of the liquid perfusion membrane contactor module are monitored through the pressure gauge and the flowmeter, and finally, dissolved methane in the waste water is permeated through a membrane to the carrier gas channel under the common drive of a chemical level difference provided by perfusion liquid and a gas partial pressure difference provided by carrier gas and is collected by the air storage tank; the liquid pouring film contactor module comprises a two-sided clamping device and a liquid pouring film; the middle part of the inner side of the clamping device is a cubic groove, two threaded round holes communicated with two ends of the groove are respectively arranged on the outer side of the clamping device, and the clamping device is externally connected with a quick plug and is used as a water inlet, a water outlet, an air inlet and an air outlet; the liquid infusion membrane comprises a porous base membrane and an infusion liquid, the infusion liquid being confined within the porous base membrane; the liquid filling film is fixed between the two clamping devices through screws and silica gel gaskets, and an anaerobic wastewater channel and a carrier gas channel are respectively formed by the liquid filling film and the inner walls of grooves of the clamping devices at the two sides; the porous base film is made of hydrophobic polymer such as polytetrafluoroethylene, polyvinylidene fluoride and polydimethylsiloxane; the pore diameter of the porous base membrane is 0.05-0.5 mu m; the porosity of the porous base film is 65-95%; the perfusion liquid is immiscible with water; the methane solubility in the perfusion liquid is higher than the methane solubility in water; the perfusion liquid is not volatilized under the condition of normal temperature and normal pressure; the priming liquid is compatible with the porous base membrane; the priming liquid has a greater affinity for the porous base membrane than water.
2. A membrane contactor system for recovering anaerobic effluent dissolved methane as claimed in claim 1, wherein: the system operates at a transmembrane pressure less than the critical pore pressure of the liquid in the liquid-perfused membrane pores.
3. A membrane contactor system for recovering anaerobic effluent dissolved methane as claimed in claim 1, wherein: the system operates with a gas-to-liquid flow ratio greater than 0.48.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5236474A (en) * | 1991-09-13 | 1993-08-17 | Bend Research, Inc. | Membrane-based removal of condensable vapors |
| US20160206993A1 (en) * | 2015-01-21 | 2016-07-21 | Liyuan DENG | Closed cycle continuous membrane ionic liquids absorption/desorption process for co2 capture |
| CN112194250A (en) * | 2020-11-06 | 2021-01-08 | 天津城建大学 | System and method for recycling biogas energy in organic wastewater anaerobic membrane biological treatment |
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- 2021-05-18 CN CN202110537693.8A patent/CN115367838B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5236474A (en) * | 1991-09-13 | 1993-08-17 | Bend Research, Inc. | Membrane-based removal of condensable vapors |
| US20160206993A1 (en) * | 2015-01-21 | 2016-07-21 | Liyuan DENG | Closed cycle continuous membrane ionic liquids absorption/desorption process for co2 capture |
| CN112194250A (en) * | 2020-11-06 | 2021-01-08 | 天津城建大学 | System and method for recycling biogas energy in organic wastewater anaerobic membrane biological treatment |
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