CN111943298A - Solar air sweeping membrane distillation system - Google Patents
Solar air sweeping membrane distillation system Download PDFInfo
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- CN111943298A CN111943298A CN202010822103.1A CN202010822103A CN111943298A CN 111943298 A CN111943298 A CN 111943298A CN 202010822103 A CN202010822103 A CN 202010822103A CN 111943298 A CN111943298 A CN 111943298A
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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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/08—Thin film evaporation
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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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/14—Treatment of water, waste water, or sewage by heating by distillation or evaporation using solar energy
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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
- Y02A20/20—Controlling water pollution; Waste water treatment
- Y02A20/208—Off-grid powered water treatment
- Y02A20/212—Solar-powered wastewater sewage treatment, e.g. spray evaporation
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Abstract
The invention discloses a solar air sweeping membrane distillation system, which comprises a solar heat collector and a feed liquid tank, wherein the solar heat collector is connected with the feed liquid tank; a hollow fiber membrane module heat exchanger and a direct contact condenser; the system of the invention effectively utilizes cheap energy and reduces the cost of water production; the heat exchange is directly carried out by utilizing a steam-water interface, and the latent heat of condensation is recovered by preheating raw material water, so that the heat transfer coefficient of the condenser is greatly improved, the heat exchange area of a metal heat exchanger is reduced while high-non-condensable gas proportion mixed steam is effectively condensed, and the cost of the condenser is reduced; the distributor is used for dispersing mixed steam or cooling water, the steam-water interface heat exchange area is obviously increased, various direct contact condensers are adopted, the steam-liquid contact area and the contact time are further increased, and the condensation efficiency is improved; the hollow fiber membrane components are connected in series, the circulating temperature of the feed liquid is reduced step by step, and the heat cycle utilization rate of the system is effectively improved; the invention recovers the heat energy of the discharged concentrated water, is used for preheating the raw material water, improves the heat utilization rate of the system and reduces the energy consumption of the system.
Description
Technical Field
The invention belongs to the technical field of water treatment and membrane separation, relates to the technical field of heat exchanger structures, and particularly relates to a solar air sweeping membrane distillation system combined with a direct contact condenser.
Background
The Membrane Distillation (MD) technology combines the traditional distillation separation technology with the membrane separation technology, and utilizes the hydrophobicity and certain structural functions of a polymer membrane to achieve the distillation concentration of the solution. The membrane distillation technology is a non-isothermal physical separation technology, and realizes transmembrane transmission of water vapor by taking the vapor pressure difference on two sides of a hydrophobic porous membrane as a driving force, and the water vapor is condensed into fresh water on a cold side. Unlike two traditional processes, membrane distillation does not need to heat the solution to boiling state, and does not need high operation pressure, and distillation separation can be realized as long as proper temperature difference is maintained on two sides of the membrane, so the operation temperature is much lower than that of the traditional distillation process, the operation pressure is much lower than that of the traditional membrane separation technology, the membrane distillation process is almost performed under normal pressure, and geothermal energy, solar energy, industrial wastewater residual heat and other cheap energy sources can be effectively utilized.
The membrane distillation technology has many advantages when applied to the field of water treatment, such as small equipment volume, low cost, milder operation temperature and pressure, good chemical stability, and the theoretical retention rate of nonvolatile components of the membrane distillation technology can reach 100 percent, and can be used for treating and separating heat-sensitive substances and high-concentration wastewater.
The air swept membrane distillation is a typical membrane distillation technology, air is used for sweeping steam on a permeation side, mass transfer resistance is effectively reduced, membrane flux is increased, and meanwhile, the advantages of the air swept membrane distillation on operation conditions are more obvious, the feeding temperature is generally about 70 ℃, and the separation process is normal-pressure operation, so that the equipment energy consumption is lower, the operation is more stable, and the air swept membrane distillation is particularly suitable for the fields of medium-small scale seawater desalination and wastewater treatment. However, based on the process characteristics, the existence of the high-proportion non-condensable gas in the steam increases the heat transfer resistance in the condensation process, the effective condensation can be realized only by increasing the heat exchange area by more than 10 times by adopting the traditional dividing wall type heat exchanger, and the high cost of the condensation equipment becomes the bottleneck restricting the technical development.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide the solar air swept membrane distillation system which effectively utilizes low-cost energy, reduces the water production cost of the system, reduces the energy consumption and effectively improves the heat cycle utilization rate of the system.
It is a second object of the present invention to provide a second solar air swept membrane distillation system.
It is a third object of the present invention to provide a third solar air swept membrane distillation system.
The technical scheme of the invention is summarized as follows:
a solar air-swept membrane distillation system comprises a first solar heat collector 1, wherein a circulating water outlet of the first solar heat collector 1 is connected with a first pump 3 through a pipeline and then is connected with a heat transfer pipe inlet of a first material liquid tank 4, and a heat transfer pipe outlet of the first material liquid tank 4 is connected with a circulating water inlet of the first solar heat collector 1 through a pipeline; the first hollow fiber membrane component group 2 comprises 1-10 hollow fiber membrane components, when the number of the hollow fiber membrane components is more than 1, the membrane filament shell pass outlet of the first hollow fiber membrane component is sequentially connected with the membrane filament shell pass inlets of the adjacent hollow fiber membrane components through a pipeline, and the membrane filament tube pass inlet of the first hollow fiber membrane component is sequentially connected with the membrane filament tube pass outlets of the adjacent hollow fiber membrane components through a pipeline; a feed liquid outlet of the first feed liquid tank 4 is connected with the second pump 5 through a pipeline and then is connected with a membrane filament tube pass inlet of the last hollow fiber membrane component of the first hollow fiber membrane component group 2, a membrane filament tube pass outlet of the first hollow fiber membrane component is divided into two paths through a pipeline, one path is connected with a concentrated water inlet of the first feed liquid tank 4, the other path is connected with a hot fluid inlet of the first heat exchanger 6, and a hot fluid outlet of the first heat exchanger 6 is connected with a concentrated water discharge pipe through a pipeline; the first air blower 7 is connected with a first hollow fiber membrane module membrane filament shell pass inlet of the first hollow fiber membrane module group 2 through a pipeline; the membrane filament shell pass outlet of the last hollow fiber membrane module is connected with the steam inlet 31 of the bubbling type direct contact condenser 10 through a pipeline and then connected with the gas disperser 32; the gas outlet 33 of the bubbling direct contact condenser is used for purge gas discharge; a raw material water pipe is connected with a coil heat exchanger inlet 35 of a coil heat exchanger 34 in the bubbling type direct contact condenser 10 through a third pump 8, a coil heat exchanger outlet 36 is divided into two paths through a pipeline, one path is a cooling water discharge pipe, the other path is connected with a cold fluid inlet of a first heat exchanger 6 through a pipeline, and a cold fluid outlet of the first heat exchanger 6 is connected with a feed liquid inlet of a first feed liquid tank 4 through a pipeline; the cooling water outlet 37 of the bubbling type direct contact condenser 10 is connected to the product water pipe after being connected to the fourth pump 9 through a pipe.
The gas disperser is preferably a plate type gas disperser, a spherical gas disperser, a pure titanium aerator, a diaphragm type aerator, a corundum aerator or a gas nozzle.
The first heat exchanger is preferably a plate heat exchanger, a shell-and-tube heat exchanger or a finned heat exchanger.
The second solar air-swept membrane distillation system comprises a second solar heat collector 11, wherein a circulating water outlet of the second solar heat collector 11 is connected with a heat transfer pipe inlet of a second material liquid tank 14 after being connected with a fifth pump 13 through a pipeline, and a heat transfer pipe outlet of the second material liquid tank 14 is connected with a circulating water inlet of the second solar heat collector 11 through a pipeline; the second hollow fiber membrane module group 12 comprises 1-20 hollow fiber membrane modules, when the number of the hollow fiber membrane modules is more than 1, the membrane filament shell pass outlet of the first hollow fiber membrane module is sequentially connected with the membrane filament shell pass inlet of the adjacent hollow fiber membrane module through a pipeline, and the membrane filament tube pass inlet of the first hollow fiber membrane module is sequentially connected with the membrane filament tube pass outlet of the adjacent hollow fiber membrane module through a pipeline; a feed liquid outlet of the second feed liquid tank 14 is connected with a sixth pump 15 through a pipeline and then is connected with a membrane filament tube pass inlet of the last hollow fiber membrane module of the second hollow fiber membrane module group 12, a membrane filament tube pass outlet of the first hollow fiber membrane module is divided into two paths through a pipeline, one path is connected with a concentrated water inlet of the second feed liquid tank 14, the other path is connected with a hot fluid inlet of a second heat exchanger 16, and a hot fluid outlet of the second heat exchanger 16 discharges concentrated water through a pipeline; the second blower 17 is connected with the first hollow fiber membrane module membrane shell pass inlet of the second hollow fiber membrane module group 12 through a pipeline, and the membrane shell pass outlet of the last hollow fiber membrane module is connected with the steam inlet 38 of the spray type direct contact condenser 20 through a pipeline; the middle part of the spray type direct contact condenser 20 is provided with a filler 39, a spray type direct contact condenser gas outlet 40 is used for discharging purge gas, a cooling water pipeline is connected with a seventh pump 43 and then connected with a liquid disperser 41 in the spray type direct contact condenser 20, a spray type direct contact condenser liquid outlet 42 is connected with a hot fluid inlet of a third heat exchanger 44 after being connected with an eighth pump 19 through a pipeline, and a hot fluid outlet of the third heat exchanger 44 is connected with a product water pipe; the raw material water is connected with the ninth pump 18 through a pipeline and then connected with a cold fluid inlet of the third heat exchanger 44, a cold fluid outlet of the third heat exchanger 44 is connected with a cold fluid inlet of the second heat exchanger 16 through a pipeline, and a cold fluid outlet of the second heat exchanger 16 is connected with a feed liquid inlet of the second feed liquid tank 14 through a pipeline.
The filler is preferably honeycomb integral filler, corrugated integral filler, ceramic filler, annular filler, saddle filler or spherical filler; the liquid disperser is a solid cone nozzle, a hollow cone nozzle or a fan-shaped nozzle.
The second heat exchanger is a plate heat exchanger, a shell-and-tube heat exchanger or a finned heat exchanger; the third heat exchanger is a plate heat exchanger, a shell-and-tube heat exchanger or a finned heat exchanger.
The third solar air-swept membrane distillation system comprises a third solar heat collector 21, wherein a circulating water outlet of the third solar heat collector 21 is connected with a tenth pump 23 through a pipeline and then is connected with a heat transfer pipe inlet of a third material liquid tank 24, and a heat transfer pipe outlet of the third material liquid tank 24 is connected with a circulating water inlet of the third solar heat collector 21 through a pipeline; the third hollow fiber membrane module group 22 comprises 1-20 hollow fiber membrane modules, when the number of the hollow fiber membrane modules is more than 1, the membrane filament shell pass outlet of the first hollow fiber membrane module is sequentially connected with the membrane filament shell pass inlets of the adjacent hollow fiber membrane modules through a pipeline, and the membrane filament tube pass inlet of the first hollow fiber membrane module is sequentially connected with the membrane filament tube pass outlets of the adjacent hollow fiber membrane modules through a pipeline; a feed liquid outlet of the third feed liquid tank 24 is connected with an eleventh pump 25 through a pipeline and then connected with a membrane filament tube pass inlet of the last hollow fiber membrane module of the third hollow fiber membrane module group 22, a membrane filament tube pass outlet of the first hollow fiber membrane module is divided into two paths through a pipeline, one path is connected with a concentrated water inlet of the third feed liquid tank 24, the other path is connected with a hot fluid inlet of the fourth heat exchanger 26, and a hot fluid outlet of the fourth heat exchanger 26 discharges concentrated water through a pipeline; the third blower 27 is connected with the first hollow fiber membrane module membrane shell pass inlet of the third hollow fiber membrane module group 22 through a pipeline, and the membrane shell pass outlet of the last hollow fiber membrane module is connected with the steam inlet 46 of the jet direct contact condenser 30 through a pipeline; a gas outlet 48 at the top of the jet direct contact condenser is used for discharging purge gas, cooling water is connected with a liquid disperser 47 of the jet direct contact condenser 30 through a pipeline by a twelfth pump 49, a liquid outlet 45 of the jet direct contact condenser is connected with a thirteenth pump 29 through a pipeline and then connected with a hot fluid inlet of a fifth heat exchanger 50, a hot fluid outlet of the fifth heat exchanger 50 is connected with a product water pipe, raw material water is connected with a cold fluid inlet of the fifth heat exchanger 50 after being connected with a fourteenth pump 28 through a pipeline, a cold fluid outlet of the fifth heat exchanger 50 is connected with a cold fluid inlet of the fourth heat exchanger 26 through a pipeline, and a cold fluid outlet of the fourth heat exchanger 26 is connected with a feed liquid inlet of the third feed liquid tank 24 through a pipeline.
The liquid disperser is a pressure atomizing nozzle, a gas-liquid two-phase flow atomizing nozzle or a high-speed centrifugal atomizing nozzle.
And a gas outlet of the condenser is provided with a gas-liquid separator which is a wire mesh type or a folded plate type.
The fourth heat exchanger is a plate type, shell-and-tube type or finned heat exchanger; the fifth heat exchanger is a plate type, shell-and-tube type or finned heat exchanger.
The invention has the advantages and positive effects that:
1. the solar energy water heater adopts the solar heat collector as a system heat source, effectively utilizes low-price energy and reduces the water production cost of the system.
2. The invention utilizes the direct heat exchange of the steam-water interface to replace the traditional dividing wall type heat exchange, recovers the latent heat of condensation by preheating the raw material water, greatly improves the heat transfer coefficient of the condenser, reduces the heat exchange area of the metal heat exchanger while effectively condensing the mixed steam with high non-condensable gas ratio, and reduces the cost of the condenser.
3. The invention utilizes the distributor to disperse the mixed steam or cooling water, can obviously increase the heat exchange area of the steam-water interface, adopts a direct contact condenser in the forms of injection, bead, film, bubble and the like, further increases the contact area and contact time of the steam and the liquid, and improves the condensation efficiency.
4. The hollow fiber membrane components are connected in series, the circulating temperature of the feed liquid is reduced step by step, and the heat cycle utilization rate of the system is effectively improved.
5. The invention recovers the heat energy of the discharged concentrated water, is used for preheating the raw material water, improves the heat utilization rate of the system and reduces the energy consumption of the system.
Drawings
FIG. 1 is a schematic view of a first solar air swept membrane distillation system;
FIG. 2 is a schematic view of a second solar air swept membrane distillation system;
FIG. 3 is a schematic view of a third solar air swept membrane distillation system.
Detailed Description
The present invention is described in further detail below with reference to the attached drawings and the detailed description, and it should be noted that the following examples are illustrative only, are intended to provide further explanation of the present invention, and are not restrictive, and the protection scope of the present invention should not be limited thereby.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments according to the present application. As used herein, the singular is intended to include the plural unless the context clearly dictates otherwise.
A solar air-swept membrane distillation system is shown in figure 1 and comprises a first solar heat collector 1, wherein a circulating water outlet of the first solar heat collector 1 is connected with a first pump 3 through a pipeline and then connected with a heat transfer pipe inlet of a first material liquid tank 4, and a heat transfer pipe outlet of the first material liquid tank 4 is connected with a circulating water inlet of the first solar heat collector 1 through a pipeline; the first hollow fiber membrane module group 2 includes 2 hollow fiber membrane modules, (in this embodiment, 2 are taken as an example, one number may be selected from 1 or 3 to 20, such as 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19 or 20), when the number of the hollow fiber membrane modules is greater than 1, a membrane filament shell pass outlet of a first hollow fiber membrane module is sequentially connected with a membrane filament shell pass inlet of an adjacent hollow fiber membrane module through a pipeline, and a membrane filament tube pass inlet of the first hollow fiber membrane module is sequentially connected with a membrane filament tube pass outlet of the adjacent hollow fiber membrane module through a pipeline; a feed liquid outlet of the first feed liquid tank 4 is connected with the second pump 5 through a pipeline and then is connected with a membrane filament tube pass inlet of the last hollow fiber membrane component of the first hollow fiber membrane component group 2, a membrane filament tube pass outlet of the first hollow fiber membrane component is divided into two paths through a pipeline, one path is connected with a concentrated water inlet of the first feed liquid tank 4, the other path is connected with a hot fluid inlet of the first heat exchanger 6, and a hot fluid outlet of the first heat exchanger 6 is connected with a concentrated water discharge pipe through a pipeline; the first air blower 7 is connected with a first hollow fiber membrane module membrane filament shell pass inlet of the first hollow fiber membrane module group 2 through a pipeline; the membrane filament shell pass outlet of the last hollow fiber membrane module is connected with the steam inlet 31 of the bubbling type direct contact condenser 10 through a pipeline and then connected with the gas disperser 32; the gas outlet 33 of the bubbling direct contact condenser is used for purge gas discharge; a raw material water pipe is connected with a coil heat exchanger inlet 35 of a coil heat exchanger 34 in the bubbling type direct contact condenser 10 through a third pump 8, a coil heat exchanger outlet 36 is divided into two paths through a pipeline, one path is a cooling water discharge pipe, the other path is connected with a cold fluid inlet of a first heat exchanger 6 through a pipeline, and a cold fluid outlet of the first heat exchanger 6 is connected with a feed liquid inlet of a first feed liquid tank 4 through a pipeline; the cooling water outlet 37 of the bubbling type direct contact condenser 10 is connected to the product water pipe after being connected to the fourth pump 9 through a pipe.
The gas disperser is preferably a plate type gas disperser, and can also be a spherical gas disperser, a pure titanium aerator, a diaphragm type aerator, a corundum aerator or a gas nozzle.
The first heat exchanger is preferably a plate heat exchanger, and can also be a shell-and-tube heat exchanger or a finned heat exchanger.
A second solar air-swept membrane distillation system, as shown in fig. 2, comprises a second solar heat collector 11, wherein a circulating water outlet of the second solar heat collector 11 is connected with a fifth pump 13 through a pipeline and then connected with an inlet of a heat transfer pipe of a second feed liquid tank 14, and an outlet of the heat transfer pipe of the second feed liquid tank 14 is connected with a circulating water inlet of the second solar heat collector 11 through a pipeline; the second hollow fiber membrane module group 12 includes 2 hollow fiber membrane modules, (in this embodiment, 2 are taken as an example, one number may be selected from 1 or 3 to 20, such as 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19 or 20), when the number of the hollow fiber membrane modules is greater than 1, the membrane filament shell pass outlet of the first hollow fiber membrane module is sequentially connected with the membrane filament shell pass inlet of the adjacent hollow fiber membrane module through a pipeline, and the membrane filament tube pass inlet of the first hollow fiber membrane module is sequentially connected with the membrane filament tube pass outlet of the adjacent hollow fiber membrane module through a pipeline; a feed liquid outlet of the second feed liquid tank 14 is connected with a sixth pump 15 through a pipeline and then is connected with a membrane filament tube pass inlet of the last hollow fiber membrane module of the second hollow fiber membrane module group 12, a membrane filament tube pass outlet of the first hollow fiber membrane module is divided into two paths through a pipeline, one path is connected with a concentrated water inlet of the second feed liquid tank 14, the other path is connected with a hot fluid inlet of a second heat exchanger 16, and a hot fluid outlet of the second heat exchanger 16 discharges concentrated water through a pipeline; the second blower 17 is connected with the first hollow fiber membrane module membrane shell pass inlet of the second hollow fiber membrane module group 12 through a pipeline, and the membrane shell pass outlet of the last hollow fiber membrane module is connected with the steam inlet 38 of the spray type direct contact condenser 20 through a pipeline; the middle part of the spray type direct contact condenser 20 is provided with a filler 39, a spray type direct contact condenser gas outlet 40 is used for discharging purge gas, a cooling water pipeline is connected with a seventh pump 43 and then connected with a liquid disperser 41 in the spray type direct contact condenser 20, a spray type direct contact condenser liquid outlet 42 is connected with a hot fluid inlet of a third heat exchanger 44 after being connected with an eighth pump 19 through a pipeline, and a hot fluid outlet of the third heat exchanger 44 is connected with a product water pipe; the raw material water is connected with the ninth pump 18 through a pipeline and then connected with a cold fluid inlet of the third heat exchanger 44, a cold fluid outlet of the third heat exchanger 44 is connected with a cold fluid inlet of the second heat exchanger 16 through a pipeline, and a cold fluid outlet of the second heat exchanger 16 is connected with a feed liquid inlet of the second feed liquid tank 14 through a pipeline.
The packing is preferably a honeycomb structured packing, and may also be selected from a corrugated structured packing, a ceramic packing, a ring packing, a saddle packing or a spherical packing.
The liquid disperser is solid cone nozzle, or hollow cone nozzle or fan nozzle.
The second heat exchanger is a plate heat exchanger, and can also be a shell-and-tube heat exchanger or a finned heat exchanger.
The third heat exchanger is a plate heat exchanger, and can also be a shell-and-tube heat exchanger or a finned heat exchanger.
The third solar air-swept membrane distillation system, as shown in fig. 3, comprises a third solar heat collector 21, wherein a circulating water outlet of the third solar heat collector 21 is connected with a tenth pump 23 through a pipeline and then connected with a heat transfer pipe inlet of a third feed liquid tank 24, and a heat transfer pipe outlet of the third feed liquid tank 24 is connected with a circulating water inlet of the third solar heat collector 21 through a pipeline; the third hollow fiber membrane module group 22 includes 2 hollow fiber membrane modules, (in this embodiment, 2 are taken as an example, one number may be selected from 1 or 3 to 20, such as 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19 or 20), when the number of the hollow fiber membrane modules is greater than 1, a membrane filament shell pass outlet of a first hollow fiber membrane module is sequentially connected with a membrane filament shell pass inlet of an adjacent hollow fiber membrane module through a pipeline, and a membrane filament tube pass inlet of the first hollow fiber membrane module is sequentially connected with a membrane filament tube pass outlet of the adjacent hollow fiber membrane module through a pipeline; a feed liquid outlet of the third feed liquid tank 24 is connected with an eleventh pump 25 through a pipeline and then connected with a membrane filament tube pass inlet of the last hollow fiber membrane module of the third hollow fiber membrane module group 22, a membrane filament tube pass outlet of the first hollow fiber membrane module is divided into two paths through a pipeline, one path is connected with a concentrated water inlet of the third feed liquid tank 24, the other path is connected with a hot fluid inlet of the fourth heat exchanger 26, and a hot fluid outlet of the fourth heat exchanger 26 discharges concentrated water through a pipeline; the third blower 27 is connected with the first hollow fiber membrane module membrane shell pass inlet of the third hollow fiber membrane module group 22 through a pipeline, and the membrane shell pass outlet of the last hollow fiber membrane module is connected with the steam inlet 46 of the jet direct contact condenser 30 through a pipeline; a gas outlet 48 (provided with a gas-liquid separator at an outlet) at the top of the jet direct contact condenser is used for discharging purge gas, cooling water is connected with a liquid disperser 47 of the jet direct contact condenser 30 through a twelfth pump 49 by a pipeline, a liquid outlet 45 of the jet direct contact condenser is connected with a thirteenth pump 29 by a pipeline and then connected with a hot fluid inlet of a fifth heat exchanger 50, a hot fluid outlet of the fifth heat exchanger 50 is connected with a product water pipe, raw material water is connected with a cold fluid inlet of the fifth heat exchanger 50 after being connected with a fourteenth pump 28 by a pipeline, a cold fluid outlet of the fifth heat exchanger 50 is connected with a cold fluid inlet of the fourth heat exchanger 26 by a pipeline, and a cold fluid outlet of the fourth heat exchanger 26 is connected with a feed liquid inlet of the third feed liquid tank 24 by a pipeline.
The liquid disperser is a pressure atomizing nozzle, and can also be a gas-liquid two-phase flow atomizing nozzle or a high-speed centrifugal atomizing nozzle.
The gas outlet of the condenser is provided with a gas-liquid separator which is a silk screen type and can also be a folding plate type.
The fourth heat exchanger is a plate heat exchanger, and can also be a shell-and-tube or finned heat exchanger;
the fifth heat exchanger is a plate heat exchanger, and can also be a shell-and-tube or finned heat exchanger.
Claims (10)
1. A solar air-swept membrane distillation system is characterized by comprising a first solar heat collector (1), wherein a circulating water outlet of the first solar heat collector (1) is connected with a first pump (3) through a pipeline and then is connected with a heat transfer pipe inlet of a first feed liquid tank (4), and a heat transfer pipe outlet of the first feed liquid tank (4) is connected with a circulating water inlet of the first solar heat collector (1) through a pipeline; the first hollow fiber membrane component group (2) comprises 1-20 hollow fiber membrane components, when the number of the hollow fiber membrane components is more than 1, the membrane filament shell pass outlet of the first hollow fiber membrane component is sequentially connected with the membrane filament shell pass inlet of the adjacent hollow fiber membrane component through a pipeline, and the membrane filament tube pass inlet of the first hollow fiber membrane component is sequentially connected with the membrane filament tube pass outlet of the adjacent hollow fiber membrane component through a pipeline; a feed liquid outlet of the first feed liquid tank (4) is connected with the second pump (5) through a pipeline and then is connected with a membrane filament tube pass inlet of the last hollow fiber membrane component of the first hollow fiber membrane component group (2), a membrane filament tube pass outlet of the first hollow fiber membrane component is divided into two paths through a pipeline, one path is connected with a concentrated water inlet of the first feed liquid tank (4), the other path is connected with a hot fluid inlet of the first heat exchanger (6), and a hot fluid outlet of the first heat exchanger (6) is connected with a concentrated water discharge pipe through a pipeline; the first air blower (7) is connected with a first hollow fiber membrane module membrane shell pass inlet of the first hollow fiber membrane module group (2) through a pipeline; the membrane filament shell pass outlet of the last hollow fiber membrane component is connected with a steam inlet (31) of the bubbling type direct contact condenser (10) through a pipeline and then connected with a gas disperser (32); the gas outlet (33) of the bubbling type direct contact condenser is used for discharging the purge gas; a raw material water pipe is connected with a coil heat exchanger inlet (35) of a coil heat exchanger (34) in the bubbling type direct contact condenser (10) through a third pump (8), a coil heat exchanger outlet (36) is divided into two paths through a pipeline, one path is a cooling water discharge pipe, the other path is connected with a cold fluid inlet of a first heat exchanger (6) through a pipeline, and a cold fluid outlet of the first heat exchanger (6) is connected with a feed liquid inlet of a first feed liquid tank (4) through a pipeline; and a cooling water outlet (37) of the bubbling type direct contact condenser (10) is connected with a product water pipe after being connected with a fourth pump (9) through a pipeline.
2. The solar air swept membrane distillation system of claim 1, wherein the gas disperser is a plate gas disperser, a spherical gas disperser, a pure titanium aerator, a membrane aerator, a corundum aerator, or a gas shower.
3. The solar air swept membrane distillation system of claim 1, wherein the first heat exchanger is a plate heat exchanger, a shell and tube heat exchanger, or a finned heat exchanger.
4. A solar air-swept membrane distillation system is characterized by comprising a second solar heat collector (11), wherein a circulating water outlet of the second solar heat collector (11) is connected with a fifth pump (13) through a pipeline and then is connected with an inlet of a heat transfer pipe of a second feed liquid tank (14), and an outlet of the heat transfer pipe of the second feed liquid tank (14) is connected with a circulating water inlet of the second solar heat collector (11) through a pipeline; the second hollow fiber membrane component group (12) comprises 1-20 hollow fiber membrane components, when the number of the hollow fiber membrane components is more than 1, the membrane filament shell pass outlet of the first hollow fiber membrane component is sequentially connected with the membrane filament shell pass inlet of the adjacent hollow fiber membrane component through a pipeline, and the membrane filament tube pass inlet of the first hollow fiber membrane component is sequentially connected with the membrane filament tube pass outlet of the adjacent hollow fiber membrane component through a pipeline; a feed liquid outlet of the second feed liquid tank (14) is connected with a sixth pump (15) through a pipeline and then is connected with a membrane filament tube pass inlet of the last hollow fiber membrane component of the second hollow fiber membrane component group (12), a membrane filament tube pass outlet of the first hollow fiber membrane component is divided into two paths through a pipeline, one path is connected with a concentrated water inlet of the second feed liquid tank (14), the other path is connected with a hot fluid inlet of a second heat exchanger (16), and a hot fluid outlet of the second heat exchanger (16) discharges concentrated water through a pipeline; the second air blower (17) is connected with a first hollow fiber membrane module shell pass inlet of a second hollow fiber membrane module group (12) through a pipeline, and a membrane shell pass outlet of a last hollow fiber membrane module is connected with a steam inlet (38) of the spray type direct contact condenser (20) through a pipeline; the middle part of the spray type direct contact condenser (20) is provided with a filler (39), a gas outlet (40) of the spray type direct contact condenser is used for discharging purge gas, a cooling water pipeline is connected with a seventh pump (43) and then connected with a liquid disperser (41) in the spray type direct contact condenser (20), a liquid outlet (42) of the spray type direct contact condenser is connected with a hot fluid inlet of a third heat exchanger (44) after being connected with an eighth pump (19) through a pipeline, and a hot fluid outlet of the third heat exchanger (44) is connected with a product water pipe; the raw material water is connected with a ninth pump (18) through a pipeline and then is connected with a cold fluid inlet of a third heat exchanger (44), a cold fluid outlet of the third heat exchanger (44) is connected with a cold fluid inlet of a second heat exchanger (16) through a pipeline, and a cold fluid outlet of the second heat exchanger (16) is connected with a feed liquid inlet of a second feed liquid tank (14) through a pipeline.
5. The solar air swept membrane distillation system of claim 4, wherein the packing is honeycomb structured packing, corrugated structured packing, ceramic packing, ring packing, saddle packing, or spherical packing; the liquid disperser is a solid cone nozzle, a hollow cone nozzle or a fan-shaped nozzle.
6. The solar air swept membrane distillation system of claim 4, wherein the second heat exchanger is a plate heat exchanger, a shell and tube heat exchanger, or a finned heat exchanger; the third heat exchanger is a plate heat exchanger, a shell-and-tube heat exchanger or a finned heat exchanger.
7. A solar air-swept membrane distillation system is characterized by comprising a third solar heat collector (21), wherein a circulating water outlet of the third solar heat collector (21) is connected with a tenth pump (23) through a pipeline and then is connected with an inlet of a heat transfer pipe of a third material liquid tank (24), and an outlet of the heat transfer pipe of the third material liquid tank (24) is connected with a circulating water inlet of the third solar heat collector (21) through a pipeline; the third hollow fiber membrane component group (22) comprises 1-20 hollow fiber membrane components, when the number of the hollow fiber membrane components is more than 1, the membrane filament shell pass outlet of the first hollow fiber membrane component is sequentially connected with the membrane filament shell pass inlet of the adjacent hollow fiber membrane component through a pipeline, and the membrane filament tube pass inlet of the first hollow fiber membrane component is sequentially connected with the membrane filament shell pass outlet of the adjacent hollow fiber membrane component through a pipeline; a feed liquid outlet of the third feed liquid tank (24) is connected with an eleventh pump (25) through a pipeline and then is connected with a membrane filament tube pass inlet of the last hollow fiber membrane component of the third hollow fiber membrane component group (22), a membrane filament tube pass outlet of the first hollow fiber membrane component is divided into two paths through a pipeline, one path is connected with a concentrated water inlet of the third feed liquid tank (24), the other path is connected with a hot fluid inlet of a fourth heat exchanger (26), and a hot fluid outlet of the fourth heat exchanger (26) discharges concentrated water through a pipeline; the third air blower (27) is connected with a first hollow fiber membrane module shell side inlet of a third hollow fiber membrane module group (22) through a pipeline, and a membrane shell side outlet of a last hollow fiber membrane module is connected with a steam inlet (46) of the jet direct contact condenser (30) through a pipeline; the top gas outlet (48) of the jet direct contact condenser is used for discharging purge gas, cooling water is connected with a liquid disperser (47) of the jet direct contact condenser (30) through a twelfth pump (49) through a pipeline, a liquid outlet (45) of the jet direct contact condenser is connected with a thirteenth pump (29) through a pipeline and then connected with a hot fluid inlet of a fifth heat exchanger (50), a hot fluid outlet of the fifth heat exchanger (50) is connected with a product water pipe, raw material water is connected with a fourteenth pump (28) through a pipeline and then connected with a cold fluid inlet of the fifth heat exchanger (50), a cold fluid outlet of the fifth heat exchanger (50) is connected with a cold fluid inlet of a fourth heat exchanger (26) through a pipeline, and a cold fluid outlet of the fourth heat exchanger (26) is connected with a feed liquid inlet of a third feed liquid tank (24) through a pipeline.
8. The solar air swept membrane distillation system of claim 7, wherein the liquid disperser is a pressure atomizing nozzle, a gas-liquid two-phase flow atomizing nozzle, or a high speed centrifugal atomizing nozzle.
9. The solar air swept membrane distillation system of claim 7, wherein the condenser gas outlet is provided with a vapor-liquid separator, and the vapor-liquid separator is of a wire mesh type or a folded plate type.
10. The solar air swept membrane distillation system of claim 7, wherein the fourth heat exchanger is a plate, shell and tube or finned heat exchanger; the fifth heat exchanger is a plate type, shell-and-tube type or finned heat exchanger.
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| CN113731178A (en) * | 2021-08-24 | 2021-12-03 | 自然资源部天津海水淡化与综合利用研究所 | Adopt gas of series connection feeding to sweep membrane distillation system |
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Application publication date: 20201117 |