CN112387122A - Microchannel membrane distillation assembly and apparatus and method for enhancing membrane distillation transfer process using microchannels - Google Patents

Microchannel membrane distillation assembly and apparatus and method for enhancing membrane distillation transfer process using microchannels Download PDF

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CN112387122A
CN112387122A CN202011258875.3A CN202011258875A CN112387122A CN 112387122 A CN112387122 A CN 112387122A CN 202011258875 A CN202011258875 A CN 202011258875A CN 112387122 A CN112387122 A CN 112387122A
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membrane distillation
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joint
microchannel
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CN112387122B (en
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金央
魏志桢
任永胜
李军
刘肖
陈明
贾连玉
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Sichuan University
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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
    • B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
    • B01D61/364—Membrane distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
    • B01D61/366—Apparatus therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/02—Hollow fibre modules
    • B01D63/028—Microfluidic devices comprising semi-permeable hollow fibre membranes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/08—Prevention of membrane fouling or of concentration polarisation

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Abstract

According to the microchannel membrane distillation assembly, a first capillary inner hole, a hydrophobic microporous hollow fiber membrane inner hole and a second capillary inner hole form a tube-side microchannel, and an annular space between the outer wall of the hydrophobic microporous hollow fiber membrane and the inner wall of an outer tube forms a shell-side microchannel. The microchannel membrane distillation device comprises the microchannel membrane distillation component, a feed liquid circulating tank, a heating water bath, a first delivery pump, an electronic balance, a cold liquid collecting tank, a conductivity meter, a second delivery pump, a constant temperature water bath, a computer and a temperature sensor. The invention relates to a method for strengthening a membrane distillation transfer process by using a microchannel, which uses the microchannel membrane distillation device to carry out membrane distillation operation. The invention provides different technical concepts for exploring and developing a method for strengthening the membrane distillation transfer process, weakening the polarization phenomenon and improving the membrane flux.

Description

Microchannel membrane distillation assembly and apparatus and method for enhancing membrane distillation transfer process using microchannels
Technical Field
The invention belongs to the technical field of membrane distillation, and particularly relates to a membrane distillation assembly, a membrane distillation device and a method for strengthening a membrane distillation transfer process.
Background
As a new membrane separation technology, membrane distillation is widely applied to the aspects of food processing, seawater desalination, wastewater treatment and the like. The membrane distillation is characterized in that a hydrophobic microporous membrane is used as a medium, volatile components in feed liquid permeate through membrane pores in a steam mode under the action of steam pressure difference on two sides of the membrane, so that separation is realized, and a membrane distillation assembly is the core of the membrane distillation technology.
The hollow fiber type membrane distillation component is a common membrane distillation component, the existing hollow fiber type membrane distillation component mainly comprises a shell, a plurality of hollow fiber membrane filaments positioned in the shell, and a first tube pass joint and a second tube pass joint which are respectively installed at two ends of the shell, a shell pass liquid inlet pipe and a shell pass liquid outlet pipe are respectively arranged on the side wall of the shell close to two ends, and the first tube pass joint and the second tube pass joint are respectively provided with a tube pass liquid inlet pipe and a tube pass liquid outlet pipe. Research shows that the polarization effect of the membrane distillation assembly with the structure in the membrane distillation process can reduce the driving force of heat transfer and mass transfer to a certain extent, and the membrane flux is reduced. The polarization phenomenon also makes the membrane surface more prone to crystallization than the bulk of the solution, increasing the risk of salt deposition and fouling on the membrane surface. Therefore, the weakening of the polarization phenomenon is very important for improving the performance of the membrane distillation heat and mass transfer process.
The technical measures for weakening the polarization phenomenon in the prior art are generally to increase the turbulence degree of the fluid, such as increasing the flow rate of the fluid, introducing gas, adding a baffle or a spacer, and the like, and although the resistance in the transfer process can be reduced to a certain extent, the weakening degree of the polarization phenomenon by these macroscopic transfer process strengthening methods is very limited, and the equipment structure is complicated, the implementation manner is complicated, and the economy is poor.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a micro-channel membrane distillation assembly and a micro-channel membrane distillation device, so that the temperature polarization and concentration polarization phenomena in the membrane distillation process are effectively weakened, the membrane flux is further improved, the preparation cost is reduced, and the structure is simplified.
It is yet another object of the present invention to provide a method for enhancing membrane distillation transfer processes using microchannels.
The invention relates to a micro-channel membrane distillation assembly which comprises a base, a hydrophobic microporous hollow fiber membrane, an outer pipe, a heat insulation layer, a first tee joint, a second tee joint, a first capillary pipe, a second capillary pipe, a first two-way joint, a second two-way joint, a liquid inlet pipe and a liquid outlet pipe, wherein the outer pipe is arranged at the bottom of the base;
the center line of a second flow passage of the first tee is superposed with the center line of a third flow passage of the first tee, and the center line of a first flow passage of the first tee is perpendicular to the center lines of the second flow passage and the third flow passage of the first tee; the center line of a second flow passage of the second tee is superposed with the center line of a third flow passage of the second tee, and the center line of a first flow passage of the second tee is perpendicular to the center lines of the second flow passage and the third flow passage of the second tee; joints are arranged at the end parts of the flow passage interfaces of the first tee joint and the second tee joint, and one ends of the first two-way joint and the second two-way joint are provided with the joints;
one end of the outer pipe penetrates through a joint inner hole arranged on a third flow channel of the first tee joint and is inserted into the third flow channel and is fixed by a sealing ring combined with the third flow channel through a joint, and the other end of the outer pipe penetrates through a joint inner hole arranged on a third flow channel of the second tee joint and is inserted into the third flow channel and is fixed by a sealing ring combined with the third flow channel through a joint; the length of the hydrophobic microporous hollow fiber membrane is greater than that of the outer tube, the hydrophobic microporous hollow fiber membrane is inserted in the inner hole of the outer tube, and two ends of the hydrophobic microporous hollow fiber membrane extend out of the outer tube; one end of the first capillary tube passes through a joint inner hole arranged in a second flow passage of the first tee joint and is inserted into one end of an inner hole of the hydrophobic microporous hollow fiber membrane, the other end of the first capillary tube passes through a joint inner hole arranged in the first two-way joint and is inserted into the first two-way inner hole, and the first capillary tube is fixed by two sealing rings which are respectively combined with the second flow passage and the first two-way joint of the first tee joint through joints; one end of the second capillary tube passes through a joint inner hole arranged in a second flow passage of the second tee joint and is inserted into the other end of the inner hole of the hydrophobic microporous hollow fiber membrane, the other end of the second capillary tube passes through a joint inner hole arranged in the second two-way joint and is inserted into a second two-way inner hole, and the second capillary tube is fixed by two sealing rings which are respectively combined with the second flow passage of the second tee joint and the second two-way joint through joints; one end of the liquid inlet pipe penetrates through the joint to be inserted into a first flow channel of the first tee joint and is fixed by a sealing ring combined with the first flow channel through the joint; one end of the liquid outlet pipe penetrates through the joint to be inserted into a first flow channel of the second tee joint and is fixed by a sealing ring combined with the first flow channel through the joint; the heat-insulating layer is coated on the outer pipe, and the first tee joint and the second tee joint are fixed on the base through screws respectively;
the first capillary inner hole, the hydrophobic microporous hollow fiber membrane inner hole and the second capillary inner hole form a tube pass micro-channel, and the ends of the first two-way pipe and the second two-way pipe, which are not provided with joints, are respectively a liquid inlet and a liquid outlet of the tube pass micro-channel; an annular space between the outer wall of the hydrophobic microporous hollow fiber membrane and the inner wall of the outer pipe forms a shell-side micro-channel, and the liquid inlet pipe and the liquid outlet pipe are respectively a liquid inlet and a liquid outlet of the shell-side micro-channel.
The inner diameter of the hydrophobic microporous hollow fiber membrane of the microchannel membrane distillation component is preferably not more than 1.0mm, and the gap between the outer wall of the hydrophobic microporous hollow fiber membrane and the inner wall of the outer tube is preferably not more than 0.5 mm. The outer diameters of the first capillary and the second capillary are matched with the inner diameter of the hydrophobic microporous hollow fiber membrane.
The difference between the length of the hydrophobic microporous hollow fiber membrane and the length of the outer tube of the micro-channel membrane distillation component is at least 50 mm.
According to the microchannel membrane distillation assembly, the hydrophobic microporous hollow fiber membrane can be made of polyvinylidene fluoride (PVDF), polypropylene (PP) or Polytetrafluoroethylene (PTFE), the outer tube can be made of organic glass, quartz glass, nylon or polyethylene, and the first capillary tube and the second capillary tube can be made of stainless steel, nylon or polyethylene.
The invention relates to a microchannel membrane distillation device, which comprises a feed liquid circulating tank, a heating water bath kettle for heating feed liquid, a first delivery pump, an electronic balance, a cold liquid collecting tank, a conductivity meter, a second delivery pump, a constant temperature water bath kettle, a computer, a first temperature sensor, a second temperature sensor, a third temperature sensor, a fourth temperature sensor and a microchannel membrane distillation assembly, wherein the first delivery pump is connected with the first delivery pump; the liquid outlet of the feed liquid circulating groove is connected with the liquid inlet of a first conveying pump through a pipe fitting, the liquid outlet of the first conveying pump is connected with the shell-side micro-channel liquid inlet of the micro-channel membrane distillation assembly through a pipe fitting, and the shell-side micro-channel liquid outlet of the micro-channel membrane distillation assembly is connected with the liquid inlet of the feed liquid circulating groove through a pipe fitting to form a feed liquid loop; the liquid outlet of the cold liquid collecting tank is connected with the liquid inlet of a second conveying pump through a pipe fitting, the liquid outlet of the second conveying pump is connected with the liquid inlet of a constant-temperature water bath through a pipe fitting, the liquid outlet of the constant-temperature water bath is connected with the tube pass micro-channel liquid inlet of the micro-channel membrane distillation assembly through a pipe fitting, and the tube pass micro-channel liquid outlet of the micro-channel membrane distillation assembly is connected with the liquid inlet of the cold liquid collecting tank through a pipe fitting to form a cold liquid loop; the first temperature sensor and the second temperature sensor are respectively arranged at a shell-side micro-channel liquid inlet and a liquid outlet of the micro-channel membrane distillation assembly, and the third temperature sensor and the fourth temperature sensor are respectively arranged at a tube-side micro-channel liquid inlet and a liquid outlet of the micro-channel membrane distillation assembly; the cold liquid collecting tank is positioned on the electronic balance, the conductivity meter is used for detecting the change of the liquid conductivity in the cold liquid collecting tank, and the computer is used for receiving, processing and storing signals output by the temperature sensors, the electronic balance and the conductivity meter.
The invention relates to a method for strengthening a membrane distillation transfer process by using a microchannel, which uses the microchannel membrane distillation device to carry out membrane distillation operation. The method comprises the following steps:
firstly, starting an electronic balance, a conductivity meter, temperature sensors and a computer in the microchannel membrane distillation device;
starting a heating water bath kettle in the microchannel membrane distillation device, setting the heating temperature of the heating water bath kettle as the temperature required by the fluid at the hot side, and starting a constant temperature water bath kettle in the microchannel membrane distillation device, and setting the constant temperature of the constant temperature water bath kettle as the temperature required by the fluid at the cold side;
thirdly, heating hot side fluid in a feed liquid circulation tank of the micro-channel membrane distillation device to a required temperature by using the heating water bath, simultaneously starting a first conveying pump and a second conveying pump, and under the action of the first conveying pump, heating the hot side fluid in the feed liquid circulation tank with a flow Q2The liquid enters a shell-side microchannel of a microchannel membrane distillation assembly in the microchannel membrane distillation device for heat and mass transfer, then returns to the feed liquid circulation tank, and the cold side fluid in the cold liquid collection tank returns to the feed liquid circulation tank at a flow rate Q under the action of a second delivery pump1After reaching the required temperature by a constant temperature water bath, the water enters a tube-side micro-channel of a micro-channel membrane distillation assembly in a micro-channel membrane distillation device for heat and mass transfer, and then returns to the cold liquid collecting tank;
and fourthly, after the hot side fluid and the cold side fluid circularly flow to reach a stable state in the mode of the third step, continuously recording the data detected by the electronic balance and the conductivity meter through the computer, and calculating the membrane flux and/or the salt rejection rate of the micro-channel membrane distillation device through the obtained data.
The membrane flux is calculated as follows:
Figure BDA0002773737450000031
wherein J is the membrane flux; q is the permeation quantity in kg in time t; a is the effective membrane area in m2(ii) a t is the sampling time in h.
The salt cut-off is calculated as follows:
Figure BDA0002773737450000041
in the formula, R is the salt rejection rate; c. CfIs the concentration of solute in the hot side fluid; c. CpIs the concentration of solute in the produced water.
After the steps are finished, liquid on the hot side is replaced by deionized water, the first conveying pump and the second conveying pump are started to flush the micro-channel membrane distillation assembly in the micro-channel membrane distillation device and the internal pipeline of the device, and hot air is introduced to purge the micro-channel membrane distillation assembly, so that the inner surfaces of the tube-side micro-channel and the shell-side micro-channel are kept clean and dry.
Compared with the prior art, the invention has the following beneficial effects:
(1) the invention provides the micro-channel membrane distillation assembly for the first time, increases the types of the membrane distillation assembly, and provides different technical concepts for exploring and developing a membrane distillation transfer process for strengthening, weakening polarization phenomenon and improving membrane flux.
(2) The microchannel membrane distillation component mainly comprises an outer tube, a hydrophobic microporous hollow fiber membrane, a capillary tube, a tee joint, a two-way valve, a sealing ring and the like, and all the components can be purchased directly in the market and have lower price, so the preparation process is greatly simplified, and the manufacturing cost is reduced.
(3) The micro-channel membrane distillation assembly is simple in combination mode and easy to disassemble, so that the outer tubes, the hydrophobic microporous hollow fiber membranes and the capillary tubes with different sizes can be replaced conveniently according to needs (experiment purposes), and the sizes of the tube-side micro-channel and the shell-side micro-channel are changed.
(4) Experiments show that the microchannel membrane distillation device has higher membrane flux (see examples and comparative examples) than a membrane distillation device containing a traditional hollow fiber type membrane distillation assembly under the condition of lower flow velocity and membrane porosity, so that the mass transfer rate of the microchannel membrane distillation device is improved, the polarization phenomenon is weakened, and the transfer process is strengthened.
(5) The method for strengthening the membrane distillation transfer process by using the microchannel is realized by using the microchannel membrane distillation device, has simple operation and is convenient to popularize and use.
Drawings
FIG. 1 is a schematic structural view of a microchannel membrane distillation assembly according to the present invention;
FIG. 2 is a schematic view of the internal flow path of a microchannel membrane distillation module according to the present invention;
FIG. 3 is a schematic structural diagram of a microchannel membrane distillation apparatus according to the present invention;
FIG. 4 is a schematic diagram of a first tee and a second tee in a microchannel membrane distillation assembly according to the present invention.
In the figure, 1-1-first two-way, 1-1-1-tube side fluid outlet (liquid inlet), 1-2-second two-way, 1-2-1-tube side fluid inlet (liquid outlet), 2-1-first capillary, 2-second capillary, 3-shell side fluid inlet (liquid outlet), 4-1-first three-way, 4-1-1-first three-way first flow channel, 4-1-2-first three-way second flow channel, 4-1-3-first three-way third flow channel, 4-1-4-first screw, 4-1-5-second screw, 4-2-second three-way, 4-2-1-second three first flow channel, 4-2-second three-way second flow channel, 4-2-3-third flow channel of second tee, 4-2-4-third screw, 4-2-5-fourth screw, 5-outer tube, 6-hydrophobic microporous hollow fiber membrane, 7-insulating layer, 8-shell side fluid outlet tube (liquid inlet tube), 9-joint, 10-sealing ring, 11-base, 12-feed liquid circulation tank, 13-heating water bath kettle, 14-first delivery pump, 15-microchannel membrane distillation component, 16-electronic balance, 17-cold liquid collection tank, 18-conductivity meter, 19-second delivery pump, 20-constant temperature water bath kettle, 21-computer, 22-first temperature sensor, 23-second temperature sensor, 24-third temperature sensor, 25-fourth temperature sensor.
Detailed Description
The microchannel membrane distillation assembly, the microchannel membrane distillation apparatus and the method for enhancing the membrane distillation transfer process by using microchannels according to the present invention are further described by the following examples in combination with the accompanying drawings.
Example 1
In this embodiment, the microchannel membrane distillation assembly is composed of a base 11, a hydrophobic microporous hollow fiber membrane 6, an outer tube 5, a heat-insulating layer 7, a first tee joint 4-1, a second tee joint 4-2, a first capillary tube 2-1, a second capillary tube 2-2, a first two-way 1-1, a second two-way 1-2, a liquid inlet tube 3, a liquid outlet tube 8, a joint 9 and a sealing ring 10, as shown in fig. 1 and 2.
The hydrophobic microporous hollow fiber membrane 6 is made of polyvinylidene fluoride, the length is 200mm, the inner diameter is 0.8mm, the outer diameter is 1.2mm, the porosity is 0.60, and the average pore diameter of the membrane is 0.1 mu m; the outer tube 5 is made of organic glass, the length is 150mm, the inner diameter is 1.8mm, and the outer diameter is 3 mm; the first capillary tube 2-1 and the second capillary tube 2-2 are made of stainless steel, the length is 100mm, the inner diameter is 0.6mm, and the outer diameter is 0.8 mm; the material of feed liquor pipe 3 and drain pipe 8 is polytetrafluoroethylene, and the internal diameter is 1.8mm, and the external diameter is 3.0mm, and length is 15.0 mm.
The first tee joint 4-1 and the second tee joint 4-2 are shown in figure 4, the central line of a second flow channel 4-1-2 of the first tee joint 4-1 is superposed with the central line of a third flow channel 4-1-3 thereof, and the central line of a first flow channel 4-1-1 of the first tee joint 4-1 is vertical to the central lines of the second flow channel 4-1-2 and the third flow channel 4-1-3 thereof; the central line of the second flow passage 4-2-2 of the second tee joint 4-2 is coincident with the central line of the third flow passage 4-2-3, and the central line of the first flow passage 4-2-1 of the second tee joint 4-2 is vertical to the central lines of the second flow passage 4-2-2 and the third flow passage 4-2-3. Each flow passage of the first tee joint 4-1 and the second tee joint 4-2 is provided with an internal thread and a step combined with the sealing ring 10.
The heat-insulating layer 7 is composed of sanitary cotton, glass wool and tinfoil in sequence. The seal ring 10 is an annular rubber seal ring. The inner holes of the first two-way pipe 1-1 and the second two-way pipe 1-2 are stepped holes, and the large hole at one end of the first two-way pipe is a screw hole matched with the joint. The joint 9 is provided with a central hole and external threads combined with the first tee joint 4-1, the second tee joint 4-2, the first two-way joint 1-1 and the second two-way joint 1-2.
The combination mode of the components is as follows:
joints 9 are respectively arranged at the end parts of the flow channel interfaces of the first tee joint 4-1 and the second tee joint 4-2, the right end of the first two-way joint 1-1 is provided with the joint 9, the left end of the second two-way joint 1-2 is provided with the joint 9, and each joint is in threaded connection with each flow channel of the first tee joint 4-1 and the second tee joint 4-2 and is in threaded connection with the first two-way joint 1-1 and the second two-way joint 1-2;
one end of the outer tube 5 passes through a joint inner hole arranged on a third flow passage 4-1-3 of the first tee joint 4-1 to be inserted into the third flow passage 4-1-3 and is fixed by a sealing ring 10 positioned on a step of the third flow passage through a joint 9, the other end of the outer tube 5 passes through a joint inner hole arranged on a third flow passage 4-2-3 of the second tee joint 4-2 to be inserted into the third flow passage and is fixed by a sealing ring 10 positioned on the step of the third flow passage 4-2-3 through a joint; the hydrophobic microporous hollow fiber membrane 6 is inserted in the inner hole of the outer tube 5, and two ends of the hydrophobic microporous hollow fiber membrane extend out of the outer tube; the right end of the first capillary tube 2-1 passes through a joint inner hole arranged in a second flow passage 4-1-2 of the first tee joint 4-1 to be inserted into the left end of an inner hole of the hydrophobic microporous hollow fiber membrane 6, the left end of the first capillary tube 2-1 passes through a joint inner hole arranged in a first two-way 1-1 to be inserted into a first two-way 1-1 inner hole, and the first capillary tube 2-1 is fixed by two sealing rings 10 which are respectively positioned on a step of the second flow passage 4-1-2 of the first tee joint 4-1 and a step of the first two-way 1-1 through a joint; the left end of the second capillary tube 2-2 passes through a joint inner hole arranged in a second flow passage 4-2-2 of the second tee joint 4-2 to be inserted into the right end of an inner hole of the hydrophobic microporous hollow fiber membrane 6, the right end of the second capillary tube 2-2 passes through a joint inner hole arranged in a second two-way joint to be inserted into a second two-way 1-2 inner hole, and the second capillary tube 2-2 is fixed by two sealing rings 10 which are respectively positioned on a step 4-2-2 of the second flow passage 4-2 of the second tee joint 4-2 and the step 1-2 of the second two-way joint through joints; one end of the liquid inlet pipe 3 penetrates through the joint to be inserted into a first flow passage 4-1-1 of the first tee joint 4-1 and is fixed by a sealing ring 10 positioned on a step of the first flow passage 4-1-1 through the joint; one end of the liquid outlet pipe 8 penetrates through the joint to be inserted into the first flow channel 4-2-1 of the second tee joint 4-2 and is fixed by a sealing ring 10 positioned on a step of the first flow channel 4-2-1 through the joint; the heat-insulating layer 7 is coated on the outer pipe 5, the first tee joint 4-1 is fixed on the base 11 through a first screw 4-1-4 and a second screw 4-1-5, and the second tee joint 4-2 is fixed on the base 11 through a third screw 4-2-4 and a fourth screw 4-1-5;
as shown in fig. 2, each sealing ring 10 not only has a supporting and fixing function, but also has a sealing function, and by the sealing function of the sealing ring, each component is combined in the above manner, so that the inner hole of the first capillary tube 2-1, the inner hole of the hydrophobic microporous hollow fiber membrane 6 and the inner hole of the second capillary tube 2-2 form a tube-side microchannel, and the ends of the first two-way 1-1 and the second two-way 1-2, which are not provided with joints, are respectively a liquid inlet and a liquid outlet of the tube-side microchannel; an annular space between the outer wall of the hydrophobic microporous hollow fiber membrane 6 and the inner wall of the outer tube 5 forms a shell-side microchannel, and the liquid inlet tube 3 and the liquid outlet tube 8 are respectively a liquid inlet and a liquid outlet of the shell-side microchannel.
All components in this embodiment are commercially available.
Example 2
In this embodiment, as shown in fig. 3, the microchannel membrane distillation apparatus includes a feed liquid circulation tank 12, a heated water bath 13 for heating the feed liquid, a first transfer pump 14, an electronic balance 16, a cold liquid collection tank 17, a conductivity meter 18, a second transfer pump 19, a constant temperature water bath 20, a computer 21, a first temperature sensor 22, a second temperature sensor 23, a third temperature sensor 24, a fourth temperature sensor 25, and the microchannel membrane distillation module 15 having the structure described in embodiment 1.
The liquid outlet of the feed liquid circulation tank 12 is connected with the liquid inlet of a first delivery pump 14 through a pipe fitting, the liquid outlet of the first delivery pump 14 is connected with the shell-side micro-channel liquid inlet of a micro-channel membrane distillation assembly 15 through a pipe fitting, and the shell-side micro-channel liquid outlet of the micro-channel membrane distillation assembly is connected with the liquid inlet of the feed liquid circulation tank 12 through a pipe fitting to form a feed liquid loop; the liquid outlet of the cold liquid collecting tank 17 is connected with the liquid inlet of a second conveying pump 19 through a pipe fitting, the liquid outlet of the second conveying pump 19 is connected with the liquid inlet of a constant-temperature water bath 20 through a pipe fitting, the liquid outlet of the constant-temperature water bath 20 is connected with the liquid inlet of a tube side micro-channel of the micro-channel membrane distillation assembly 15 through a pipe fitting, and the liquid outlet of the tube side micro-channel of the micro-channel membrane distillation assembly 15 is connected with the liquid inlet of the cold liquid collecting tank 17 through a pipe fitting to form a cold liquid loop; the first temperature sensor 22 and the second temperature sensor 23 are respectively installed at a shell-side micro-channel liquid inlet and a liquid outlet of the micro-channel membrane distillation assembly 15, and the third temperature sensor 24 and the fourth temperature sensor 25 are respectively installed at a tube-side micro-channel liquid inlet and a liquid outlet of the micro-channel membrane distillation assembly 15; the cold liquid collecting tank 17 is positioned on the electronic balance 16, the conductivity meter 18 is used for detecting the change of the liquid conductivity in the cold liquid collecting tank, and the computer 21 is used for receiving, processing and storing the signals output by the temperature sensors, the electronic balance 16 and the conductivity meter 18.
In this embodiment, the first transfer pump 14 and the second transfer pump 19 are peristaltic pumps, model number BT100L, with a rotation speed range of 0-100rad/min, manufactured by baoding reyfield fluid science and technology limited; a heated water bath, model HH-2A, specification 220V, 50HZ, 500W, manufactured by Yongxing instruments Inc. of Beijing Kewei; a constant temperature water bath, model DZKW-4, power 500W, produced by Beijing Zhongxing Weiwei instruments Co., Ltd; an electronic balance, model BSA224S, precision range + -0.0001 g, maximum range 220g, manufactured by Saedolis (Beijing) Co., Ltd.; conductivity meter, model DDS-307, manufactured by shanghai precision scientific instruments ltd; temperature sensor, model 19HS 04056; the computer is a common PC.
Example 3
This example was operated using the microchannel membrane distillation apparatus described in example 2 for membrane distillation. The fluid at the hot side (the feed liquid to be treated) and the fluid at the cold side are both deionized water, and the flow mode is parallel flow. The operation steps are as follows:
starting an electronic balance 16, a conductivity meter 18, various temperature sensors and a computer 21 in the microchannel membrane distillation device;
secondly, starting a heating water bath 13 in the microchannel membrane distillation device, setting the heating temperature of the heating water bath to be 70 ℃ required by hot-side fluid, starting a constant-temperature water bath 20 in the microchannel membrane distillation device, and setting the constant-temperature of the constant-temperature water bath to be 20 ℃ required by cold-side fluid;
thirdly, heating hot side fluid in a feed liquid circulating tank 12 of the microchannel membrane distillation device to 70 ℃ by using the heating water bath (13), simultaneously starting a first conveying pump 14 and a second conveying pump 19, under the action of the first conveying pump 14, enabling hot side fluid in the feed liquid circulating tank 12 to enter a shell-side microchannel of a microchannel membrane distillation assembly 15 in the microchannel membrane distillation device at a flow rate of 4.5mL/min for heat and mass transfer and then return to the feed liquid circulating tank 12, and under the action of the second conveying pump 19, enabling cold side fluid in a cold liquid collecting tank 17 to enter a tube-side microchannel of the microchannel membrane distillation assembly 15 in the microchannel membrane distillation device at a flow rate of 4.5mL/min after reaching 20 ℃ through a constant temperature water bath 20 for heat and mass transfer and then return to the cold liquid collecting tank 17;
fourthly, after the hot side fluid and the cold side fluid circularly flow in the mode of the third step to reach a stable state, continuously recording the data of the electronic balance and the detection data of the conductivity meter by the computer 21 and passing throughThe obtained data were used to calculate the membrane flux of the microchannel membrane distillation apparatus. The permeation quantity Q is 2.5467g, 2.5493g and 2.5478g respectively measured under the condition that the time interval t is 8min, the effective membrane area A is the logarithmic mean area of the inner wall and the outer wall of the hollow fiber membrane, the effective length is 150mm, and the A is calculated to be 4.44 multiplied by 10-4m2. In this example, the membrane flux was 43.05 kg.m-2·h-1。
Comparative example 1
The comparative example is extracted from part of the content of the influence of the temperature on the membrane distillation performance in chapter 2.2.2.1 of research on alkali residue wastewater treatment by membrane distillation coupling crystallization technology, which is filed in 2014, 5, 29 of Liu of Beijing university of chemical industry.
The membrane distillation device used in the comparative example has a membrane distillation assembly as a hollow fiber type membrane distillation assembly in the background technology, and the specific structure is prepared from a membrane assembly 2.1.3.1 in the second chapter of the treatise on the research on alkali residue wastewater treatment by membrane distillation coupling crystallization technology, which is filed in 2014, 29.5.9 of the university of Beijing chemical industry Liu winter. The parameters of the polyvinylidene fluoride hollow fiber porous hydrophobic membrane are as follows: the length is 250mm, the outer diameter is 1.1mm, the inner diameter is 0.8mm, the porosity is 0.85, and the average pore diameter of the membrane is 0.2 mu m. The membrane area was controlled by the number of membrane filaments encapsulated in a stainless steel shell, which was set to 60 (0.024 m)2)。
The hot side feed liquid and the cold side circulating water of the proportion are pure water (deionized water), and under the conditions that the feed flow of the hot side feed liquid is 0.45L/min and the circulating water flow of the cold side is 0.45L/min, the temperature of the circulating water of the cold side is maintained at about 20 ℃, and the temperature of the inlet of the hot side feed liquid is maintained at 70 ℃. The membrane flux in this comparative example was 9.20 kg. m-2·h-1。
As can be seen from example 3 and comparative example 1, the membrane flux in example 3 was 4.68 times that in comparative example 1. Example 3 is only 3/5 from comparative example 1, comparing the flow rates of the fluids within the hollow fiber membranes. Therefore, the microchannel membrane distillation assembly obtains higher membrane flux than the traditional hollow fiber membrane distillation assembly under the conditions of lower flow velocity and lower membrane porosity, and proves that the mass transfer rate is improved, the polarization phenomenon is weakened and the transfer process is strengthened when the microchannel membrane distillation device is used for carrying out membrane distillation operation.
Example 4
This example was operated using the microchannel membrane distillation apparatus described in example 2 for membrane distillation. The fluid at the hot side (the feed liquid to be treated) and the fluid at the cold side are both deionized water, and the flow mode is parallel flow. The operation steps are as follows:
starting an electronic balance 16, a conductivity meter 18, various temperature sensors and a computer 21 in the microchannel membrane distillation device;
secondly, starting a heating water bath 13 in the microchannel membrane distillation device, setting the heating temperature of the heating water bath to be 60 ℃ required by hot-side fluid, starting a constant-temperature water bath 20 in the microchannel membrane distillation device, and setting the constant-temperature of the constant-temperature water bath to be 20 ℃ required by cold-side fluid;
thirdly, heating hot side fluid in a feed liquid circulating tank 12 of the microchannel membrane distillation device to 60 ℃ by using the heating water bath (13), simultaneously starting a first conveying pump 14 and a second conveying pump 19, under the action of the first conveying pump 14, enabling hot side fluid in the feed liquid circulating tank 12 to enter a shell-side microchannel of a microchannel membrane distillation assembly 15 in the microchannel membrane distillation device at a flow rate of 6mL/min for heat and mass transfer and then return to the feed liquid circulating tank 12, and under the action of the second conveying pump 19, enabling cold side fluid in a cold liquid collecting tank 17 to enter a tube-side microchannel of the microchannel membrane distillation assembly 15 in the microchannel membrane distillation device at a flow rate of 6mL/min for heat and mass transfer after reaching 20 ℃ through a constant temperature water bath 20 and then return to the cold liquid collecting tank 17;
and fourthly, after the hot side fluid and the cold side fluid circularly flow to reach a stable state in the mode of the third step, continuously recording the indicating number of the electronic balance and the detection data of the conductivity meter by the computer 21, and calculating the membrane flux of the micro-channel membrane distillation device according to the obtained data. The permeation quantity Q is respectively 1.2511g, 1.1988g and 1.2360g measured under the condition that the time interval t is 8min, the effective membrane area A is the logarithmic average area of the inner wall and the outer wall of the hollow fiber membrane, the effective length is 150mm, and the A is calculated to be 4.44 multiplied by 10-4m2. In this example, the membrane flux was 20.76 kg.m-2·h-1。
Comparative example 2
The comparative example is extracted from part of the content of the influence of the flow rate on the membrane distillation performance in chapter 2.2.2.2.2 of a research on the alkaline residue wastewater treatment by the membrane distillation coupling crystallization technology, which is filed in 2014, 5, 29 days of Liu of Beijing university of chemical industry. The membrane distillation apparatus used in this comparative example was the same as comparative example 1 in terms of the structure and parameters of the membrane distillation module.
The hot side feed liquid and the cold side circulating water of the proportion are pure water (deionized water), and under the conditions that the feed flow of the hot side feed liquid is 0.35L/min and the circulating water flow of the cold side is 0.35L/min, the temperature of the circulating water of the cold side is maintained at about 20 ℃, and the temperature of the inlet of the hot side feed liquid is 60 ℃. The membrane flux in this comparative example was 4.50 kg. m-2·h-1。
As can be seen from example 4 and comparative example 2, the membrane flux in example 4 was 4.61 times that in comparative example 2. The flow rate of the fluid within the hollow fiber membrane was compared and example 4 was approximately equal to comparative example 2. Therefore, the microchannel membrane distillation assembly obtains higher membrane flux than the traditional hollow fiber membrane distillation assembly under the condition of approximate flow velocity and lower membrane porosity, and proves that the mass transfer rate is improved, the polarization phenomenon is weakened and the transfer process is strengthened when the microchannel membrane distillation device is used for carrying out membrane distillation operation.

Claims (6)

1. A micro-channel membrane distillation assembly is characterized by comprising a base (11), a hydrophobic microporous hollow fiber membrane (6), an outer pipe (5), a heat preservation layer (7), a first tee joint (4-1), a second tee joint (4-2), a first capillary tube (2-1), a second capillary tube (2-2), a first two-way pipe (1-1), a second two-way pipe (1-2), a liquid inlet pipe (3) and a liquid outlet pipe (8);
the center line of a second flow channel (4-1-2) of the first tee joint (4-1) is superposed with the center line of a third flow channel (4-1-3), and the center line of a first flow channel (4-1-1) of the first tee joint (4-1) is vertical to the center lines of the second flow channel (4-1-2) and the third flow channel (4-1-3); the center line of a second flow channel (4-2-2) of the second tee joint (4-2) is superposed with the center line of a third flow channel (4-2-3), and the center line of a first flow channel (4-2-1) of the second tee joint (4-2) is vertical to the center lines of the second flow channel (4-2-2) and the third flow channel (4-2-3); joints (9) are respectively installed at the end parts of the flow channel interfaces of the first tee joint (4-1) and the second tee joint (4-2), and the joints (9) are installed at one ends of the first two-way joint (1-1) and the second two-way joint (1-2);
one end of the outer pipe (5) passes through a joint inner hole arranged on a third flow passage (4-1-3) of the first tee joint (4-1) and is inserted into the third flow passage and is fixed by a sealing ring combined with the third flow passage through a joint, and the other end of the outer pipe (5) passes through a joint inner hole arranged on the third flow passage (4-2-3) of the second tee joint (4-2) and is inserted into the third flow passage and is fixed by a sealing ring combined with the third flow passage through a joint; the length of the hydrophobic microporous hollow fiber membrane (6) is greater than that of the outer tube (5), the hydrophobic microporous hollow fiber membrane (6) is inserted into an inner hole of the outer tube (5), and two ends of the hydrophobic microporous hollow fiber membrane extend out of the outer tube; one end of the first capillary tube (2-1) passes through a joint inner hole arranged in a second flow passage (4-1-2) of the first tee joint (4-1) and is inserted into one end of an inner hole of the hydrophobic microporous hollow fiber membrane (6), the other end of the first capillary tube (2-1) passes through a joint inner hole arranged in the first two-way joint (1-1) and is inserted into a first two-way inner hole, and the first capillary tube (2-1) is fixed by two sealing rings which are respectively combined with the second flow passage (4-1-2) of the first tee joint (4-1) and the first two-way joint (1-1) through joints; one end of the second capillary tube (2-2) passes through a joint inner hole arranged in a second flow channel (4-2-2) of the second tee joint (4-2) and is inserted into the other end of the inner hole of the hydrophobic microporous hollow fiber membrane (6), the other end of the second capillary tube (2-2) passes through a joint inner hole arranged in the second two-way joint (1-2) and is inserted into a second two-way inner hole, and the second capillary tube (2-2) is fixed by two sealing rings which are respectively combined with the second flow channel (4-2-2) of the second tee joint (4-2) and the second two-way joint (1-2) through joints; one end of the liquid inlet pipe (3) penetrates through the joint to be inserted into a first flow passage (4-1-1) of the first tee joint (4-1) and is fixed by a sealing ring combined with the first flow passage (4-1-1) through the joint; one end of the liquid outlet pipe (8) is inserted into a first flow channel (4-2-1) of the second tee joint (4-2) through a joint and is fixed by a sealing ring combined with the first flow channel (4-2-1) through the joint; the heat-insulating layer (7) is coated on the outer pipe, and the first tee joint (4-1) and the second tee joint (4-2) are fixed on the base through screws respectively;
the inner hole of the first capillary tube (2-1), the inner hole of the hydrophobic microporous hollow fiber membrane (6) and the inner hole of the second capillary tube (2-2) form a tube side micro-channel, and the ends of the first two-way tube (1-1) and the second two-way tube (1-2) which are not provided with joints are respectively a liquid inlet and a liquid outlet of the tube side micro-channel; an annular space between the outer wall of the hydrophobic microporous hollow fiber membrane (6) and the inner wall of the outer tube (5) forms a shell-side micro-channel, and the liquid inlet tube (3) and the liquid outlet tube (8) are respectively a liquid inlet and a liquid outlet of the shell-side micro-channel.
2. The microchannel membrane distillation assembly according to claim 1, wherein the inner diameter of the hydrophobic microporous hollow fiber membrane (6) is not more than 1.0mm, and the gap between the outer wall of the hydrophobic microporous hollow fiber membrane (6) and the inner wall of the outer tube (5) is not more than 0.5 mm.
3. The microchannel membrane distillation assembly according to claim 1 or 2, characterized in that the difference between the length of the hydrophobic microporous hollow fiber membrane (6) and the length of the outer tube (5) is at least 50 mm.
4. A microchannel membrane distillation apparatus comprising a feed liquid circulation tank (12), a heated water bath (13) for heating the feed liquid, a first transfer pump (14), an electronic balance (16), a cold liquid collection tank (17), a conductivity meter (18), a second transfer pump (19), a constant temperature water bath (20), a computer (21), a first temperature sensor (22), a second temperature sensor (23), a third temperature sensor (24), a fourth temperature sensor (25), characterized by further comprising the microchannel membrane distillation module (15) according to any one of claims 1 to 3;
the liquid outlet of the feed liquid circulating tank (12) is connected with the liquid inlet of a first conveying pump (14) through a pipe fitting, the liquid outlet of the first conveying pump (14) is connected with the shell-side micro-channel liquid inlet of a micro-channel membrane distillation assembly (15) through a pipe fitting, and the shell-side micro-channel liquid outlet of the micro-channel membrane distillation assembly is connected with the liquid inlet of the feed liquid circulating tank (12) through a pipe fitting to form a feed liquid loop;
the liquid outlet of the cold liquid collecting tank (17) is connected with the liquid inlet of a second conveying pump (19) through a pipe fitting, the liquid outlet of the second conveying pump (19) is connected with the liquid inlet of a constant-temperature water bath (20) through a pipe fitting, the liquid outlet of the constant-temperature water bath (20) is connected with the tube side micro-channel liquid inlet of the micro-channel membrane distillation assembly (15) through a pipe fitting, and the tube side micro-channel liquid outlet of the micro-channel membrane distillation assembly (15) is connected with the liquid inlet of the cold liquid collecting tank (17) through a pipe fitting to form a cold liquid loop;
the first temperature sensor (22) and the second temperature sensor (23) are respectively arranged at a shell-side micro-channel liquid inlet and a liquid outlet of the micro-channel membrane distillation assembly (15), and the third temperature sensor (24) and the fourth temperature sensor (25) are respectively arranged at a tube-side micro-channel liquid inlet and a liquid outlet of the micro-channel membrane distillation assembly (15);
the cold liquid collecting tank (17) is positioned on the electronic balance (16), the conductivity meter (18) is used for detecting the change of the liquid conductivity in the cold liquid collecting tank, and the computer (21) is used for receiving signals output by the temperature sensors, the electronic balance (16) and the conductivity meter (18) and processing and storing the signals.
5. A method for enhancing membrane distillation transfer process by using microchannel, which is characterized in that the microchannel membrane distillation apparatus according to claim 4 is used for membrane distillation operation.
6. The method of using microchannels to enhance membrane distillation transfer processes of claim 5, wherein the steps are as follows:
opening an electronic balance (16), a conductivity meter (18), temperature sensors and a computer (21) in the microchannel membrane distillation device;
starting a heating water bath (13) in the microchannel membrane distillation device, setting the heating temperature of the heating water bath as the temperature required by the fluid at the hot side, starting a constant-temperature water bath (20) in the microchannel membrane distillation device, and setting the constant-temperature of the constant-temperature water bath as the temperature required by the fluid at the cold side;
thirdly, after the hot side fluid in the feed liquid circulation tank (12) of the micro-channel membrane distillation device is heated to the required temperature by the heating water bath (13), the first conveying pump (14) and the second conveying pump (19) are simultaneously started, and under the action of the first conveying pump (14), the hot side fluid in the feed liquid circulation tank (12) is heated at a flow rate Q2Microchannel membrane distillation assembly into microchannel membrane distillation device(15) The shell-side micro-channel returns to the feed liquid circulating tank (12) after heat and mass transfer, and the fluid on the cold side in the cold liquid collecting tank (17) is subjected to flow Q under the action of a second conveying pump (19)1After reaching the required temperature through a constant temperature water bath (20), the water enters a tube-side micro-channel of a micro-channel membrane distillation assembly (15) in the micro-channel membrane distillation device for heat and mass transfer, and then returns to the cold liquid collecting tank (17);
and fourthly, after the hot side fluid and the cold side fluid circularly flow to reach a stable state in the mode of the third step, continuously recording the data detected by the electronic balance and the conductivity meter through the computer, and calculating the membrane flux and/or the salt rejection rate of the micro-channel membrane distillation device through the obtained data.
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