CN115490383B - Membrane distillation device - Google Patents
Membrane distillation device Download PDFInfo
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- CN115490383B CN115490383B CN202211183809.3A CN202211183809A CN115490383B CN 115490383 B CN115490383 B CN 115490383B CN 202211183809 A CN202211183809 A CN 202211183809A CN 115490383 B CN115490383 B CN 115490383B
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
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- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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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
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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Abstract
The present invention provides a membrane distillation apparatus comprising: a first water inlet pipe; the inlet of the material liquid tank is connected with a first water inlet pipe; the inlet and the main outlet of the heat exchanger component are connected to the first water inlet pipe; the inlet of the membrane component is connected with the outlet of the material liquid tank through a second water inlet pipe; the inlet of the first phase-change heat storage structure is connected with the outlet of the membrane assembly through a third water inlet pipe; the inlet of the second phase change heat storage structure is connected with the outlet of the membrane component through a fourth water inlet pipe; the first return pipeline is connected between the outlet of the first phase-change heat storage structure and the inlet of the heat exchanger assembly, and the second return pipeline is connected between the outlet of the second phase-change heat storage structure and the inlet of the heat exchanger assembly; the water outlet pipe is connected with the outlet of the first fraction tank. The technical scheme of the application effectively solves the problem that a large amount of coolant is needed in the membrane distillation process in the related technology, so that the energy consumption is overlarge.
Description
Technical Field
The invention relates to the technical field of membrane distillation, in particular to a membrane distillation device.
Background
Because of the lack of fresh water resources, zero wastewater discharge is approaching. As high-strength brine increases, so too does the need for desalination technology. The membrane distillation (membrane distillation, MD) is an emerging separation technology, integrates the membrane separation technology and the low-temperature volatilization technology, has the advantages of high rejection rate, low operation temperature, capability of utilizing low-grade heat sources (such as waste heat, solar energy, wind energy, geothermal energy and the like), capability of treating high-concentration brine and the like, and has low investment cost and simple equipment, thereby attracting more and more attention. At present, a great deal of research work has been carried out on the aspects of deep concentration of reverse osmosis concentrated water, desalination of brackish water, concentration of juice and the like, and membrane distillation is considered as one of the most promising membrane separation technologies.
The driving force of MD is the vapor pressure difference at two sides of the hydrophobic microporous membrane, and the volatile substances (usually water) in the feed liquid pass through the hydrophobic membrane holes to enter the permeation side under the action of the vapor pressure difference after being vaporized at the hot side membrane surface and are condensed into liquid; non-volatile components (such as salt) are trapped by the membrane, thereby achieving the purpose of salt/water separation. As a thermal evaporation technique, there is evaporation on both the hot side and condensation on the cold side, which is a major reason for limiting the application of the membrane distillation technique, with high energy consumption. Therefore, recovery of vaporization heat to reduce energy consumption is a necessary condition for realizing industrialization of membrane distillation.
In order to realize the full utilization of heat and improve the water making ratio, the practical membrane distillation process uses the thought of multi-effect evaporation to heat the raw material liquid by using the steam penetrating through the membrane, and fully utilizes the vaporization latent heat. Because the mass transfer driving force of the membrane distillation process is the temperature difference between the two sides of the membrane, and various heat losses are accompanied, the temperature of steam penetrating through the membrane is lower than the temperature of feed liquid. The heat of the recovered steam is mostly an external heat exchanger, and also an internal heat exchanger.
In the related art, a large amount of coolant is required for both the external heat exchanger and the internal heat exchanger, which increases the consumption of energy.
Disclosure of Invention
The main purpose of the present invention is to provide a membrane distillation apparatus, so as to solve the problem that a large amount of coolant is required in the membrane distillation process in the related art, and thus the energy consumption is too large.
In order to achieve the above object, the present invention provides a membrane distillation apparatus comprising: a first water inlet pipe; the inlet of the material liquid tank is connected with the first water inlet pipe; the inlet and the main outlet of the heat exchanger assembly are connected to the first water inlet pipe; the inlet of the membrane component is connected with the outlet of the material liquid tank through a second water inlet pipe; the inlet of the first phase-change heat storage structure is connected with the outlet of the membrane component through a third water inlet pipe; the inlet of the second phase change heat storage structure is connected with the outlet of the membrane component through a fourth water inlet pipe; the fifth water inlet pipe is connected between the inlet of the first distillate tank and the outlet of the first phase-change heat storage structure, and the sixth water inlet pipe is connected between the inlet of the first distillate tank and the outlet of the second phase-change heat storage structure; the first return pipeline is connected between the outlet of the first phase-change heat storage structure and the inlet of the heat exchanger assembly, and the second return pipeline is connected between the outlet of the second phase-change heat storage structure and the inlet of the heat exchanger assembly; and the water outlet pipe is connected with the outlet of the first fraction tank.
Further, the membrane distillation apparatus further comprises: the inlet of the second fraction tank is connected with the auxiliary outlet of the heat exchanger component; and the eighth water inlet pipe is connected between the outlet of the second fraction tank and the inlet of the second phase-change heat storage structure.
Further, the heat exchanger assembly comprises a first heat exchanger and a second heat exchanger, the first heat exchanger and the second heat exchanger are both connected to the first water inlet pipe, the second heat exchanger is arranged between the first heat exchanger and the feed liquid tank, the outlet of the first phase-change heat storage structure is connected with the inlet of the first heat exchanger, the outlet of the second phase-change heat storage structure is connected with the inlet of the first heat exchanger, and the membrane distillation device further comprises a steam generator, and the steam generator is connected with the second heat exchanger.
Further, the membrane distillation device further comprises a first pump and a third return pipeline, the first end of the third return pipeline is connected with the feed liquid tank, the second end of the third return pipeline is connected with the inlet of the second heat exchanger, and the first pump is connected to the third return pipeline.
Further, the membrane distillation device further comprises a fourth return pipeline, the first end of the fourth return pipeline is connected with the inlet of the material liquid tank, and the second end of the fourth return pipeline is connected with the outlet of the membrane component.
Further, a second pump and a filter are arranged on the second water inlet pipe, and the second pump is arranged between the filter and the feed liquid tank.
Further, a first gas-liquid separator is arranged on the fifth water inlet pipe, and a second gas-liquid separator is arranged on the sixth water inlet pipe.
Further, the membrane distillation device further comprises a refrigeration device and a ninth water inlet pipe, the first end of the ninth water inlet pipe is connected with the outlet of the first gas-liquid separator and the outlet of the second gas-liquid separator, the second end of the ninth water inlet pipe is connected with the inlet of the first distillate tank, and the refrigeration device is connected to the ninth water inlet pipe.
Further, the membrane distillation apparatus further comprises a third pump connected to the ninth water inlet pipe through a suction pipe.
Further, the membrane distillation device also comprises a third gas-liquid separator which is connected to the ninth water inlet pipe and connected with the suction pipe.
By applying the technical scheme of the invention, the heat exchanger component is connected between the first water inlet pipe and the feed liquid tank, the inlet of the membrane component is connected with the outlet of the feed liquid tank through the second water inlet pipe, the inlet of the first phase-change heat storage structure is connected with the membrane component through the third water inlet pipe, and the inlet of the second phase-change heat storage structure is connected with the outlet of the membrane component through the fourth water inlet pipe. The fifth water inlet pipe is connected between the inlet of the first fraction tank and the outlet of the first phase-change heat storage structure, and the sixth water inlet pipe is connected between the inlet of the first fraction tank and the outlet of the second phase-change heat storage structure. The first return line is connected between the outlet of the first phase change heat storage structure and the inlet of the heat exchanger assembly, and the second return line is connected between the outlet of the second phase change heat storage structure and the inlet of the heat exchanger assembly. The water outlet pipe is connected with the outlet of the first fraction tank. Through the arrangement, raw water enters the heat exchanger assembly through the first water inlet pipe and is heated in the heat exchanger assembly, the heated raw water forms steam and water, and the steam and the water enter the membrane assembly to be filtered, so that fresh water is generated. Fresh water continuously runs to the first phase-change heat storage structure, the first phase-change heat storage structure absorbs heat in the fresh water, and finally the fresh water flows out through the water outlet pipe. The heat release of the first phase-change heat storage structure heats the heat exchanger component through the first return pipeline, so that the energy consumption of the heat exchanger component can be reduced. The first phase-change heat storage structure and the second phase-change heat storage structure are alternately used, namely, when the first phase-change heat storage structure releases heat, the second phase-change heat storage structure absorbs heat, and when the first phase-change heat storage structure absorbs heat, the second phase-change heat storage structure releases heat. The first phase-change heat storage structure and the second phase-change heat storage structure can heat the heat exchanger assembly respectively, so that the heat exchanger assembly can be heated continuously, and a separate heating device is not needed to heat the heat exchanger assembly. Therefore, the technical scheme effectively solves the problem that a large amount of coolant is needed in the membrane distillation process in the related technology, so that the energy consumption is overlarge.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention. In the drawings:
fig. 1 shows a schematic structural view of an embodiment of a membrane distillation apparatus according to the present invention.
Wherein the above figures include the following reference numerals:
11. a first water inlet pipe; 12. a second water inlet pipe; 121. a second pump; 122. a filter; 13. a third water inlet pipe; 14. a fourth water inlet pipe; 15. a fifth water inlet pipe; 151. a first gas-liquid separator; 16. a sixth water inlet pipe; 161. a second gas-liquid separator; 17. a first distillate tank; 18. a second distillate tank; 191. a seventh inlet pipe; 192. an eighth water inlet pipe; 20. a material liquid tank; 30. a heat exchanger assembly; 31. a first heat exchanger; 32. a second heat exchanger; 40. a membrane module; 51. a first phase change heat storage structure; 52. a second phase change heat storage structure; 61. a first return line; 62. a second return line; 63. a water outlet pipe; 64. a steam generator; 65. a first pump; 66. a third return line; 67. a fourth return line; 71. a refrigerating device; 72. a ninth water inlet pipe; 73. a third pump; 74. a suction tube; 75. and a third gas-liquid separator.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. The following description of at least one exemplary embodiment is merely exemplary in nature and is in no way intended to limit the invention, its application, or uses. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
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 in accordance with the present application. As used herein, the singular is also intended to include the plural unless the context clearly indicates otherwise, and furthermore, it is to be understood that the terms "comprises" and/or "comprising" when used in this specification are taken to specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof.
The relative arrangement of the components and steps, numerical expressions and numerical values set forth in these embodiments do not limit the scope of the present invention unless it is specifically stated otherwise. Meanwhile, it should be understood that the sizes of the respective parts shown in the drawings are not drawn in actual scale for convenience of description. Techniques, methods, and apparatus known to one of ordinary skill in the relevant art may not be discussed in detail, but are intended to be part of the specification where appropriate. In all examples shown and discussed herein, any specific values should be construed as merely illustrative, and not a limitation. Thus, other examples of the exemplary embodiments may have different values. It should be noted that: like reference numerals and letters denote like items in the following figures, and thus once an item is defined in one figure, no further discussion thereof is necessary in subsequent figures.
In the prior art, the membrane distillation process uses the thought of multi-effect evaporation to heat the raw material liquid by using the steam penetrating through the membrane, and fully utilizes the vaporization latent heat. Because the mass transfer driving force of the membrane distillation process is the temperature difference between the two sides of the membrane, and various heat losses are accompanied, the temperature of steam penetrating through the membrane is lower than the temperature of feed liquid. The heat of the recovered steam is mostly an external heat exchanger, and also an internal heat exchanger. Whether external or internal, the heat transfer occurs because the latent heat of vaporization is recovered and the heat of phase change is much greater than the sensible heat. For example, about 2500kJ/kg of heat of vaporization of water, about 4.17 kJ/(kg. ℃ C.) of specific heat, if the heat of the steam is recovered with water, 20kg of cold water is required per kg of steam for cooling (assuming a temperature difference of 30 ℃ C. Of cold water to steam). That is, if 1kg of fresh water is produced in the direct contact membrane distillation, 20kg of fresh water is required for cooling, and the water consumption is enormous. In order to solve the above technical problems.
As shown in fig. 1, in the present embodiment, the membrane distillation apparatus includes: the first water inlet pipe 11, the feed liquid tank 20, the heat exchanger assembly 30, the membrane assembly 40, the first phase change heat storage structure 51, the second phase change heat storage structure 52, the fifth water inlet pipe 15, the sixth water inlet pipe 16, the first fraction tank 17, the first return line 61, the second return line 62 and the water outlet pipe 63. The inlet of the stock solution tank 20 is connected to the first inlet pipe 11. The inlet and the main outlet of the heat exchanger assembly 30 are both connected to the first inlet conduit 11. The inlet of the membrane module 40 is connected to the outlet of the feed liquid tank 20 via the second inlet pipe 12. The inlet of the first phase change heat storage structure 51 is connected with the outlet of the membrane assembly 40 through the third water inlet pipe 13. The inlet of the second phase change heat storage structure 52 is connected to the outlet of the membrane module 40 via the fourth inlet pipe 14. The fifth water inlet pipe 15 is connected between the inlet of the first distillate tank 17 and the outlet of the first phase change heat storage structure 51, and the sixth water inlet pipe 16 is connected between the inlet of the first distillate tank 17 and the outlet of the second phase change heat storage structure 52. A first return line 61 is connected between the outlet of the first phase change heat storage structure 51 and the inlet of the heat exchanger assembly 30 and a second return line 62 is connected between the outlet of the second phase change heat storage structure 52 and the inlet of the heat exchanger assembly 30. The outlet pipe 63 is connected to the outlet of the first tank 17.
By applying the technical scheme of the invention, the heat exchanger assembly 30 is connected between the first water inlet pipe 11 and the feed liquid tank 20, the inlet of the membrane assembly 40 is connected with the outlet of the feed liquid tank 20 through the second water inlet pipe 12, the inlet of the first phase-change heat storage structure 51 is connected with the membrane assembly 40 through the third water inlet pipe 13, and the inlet of the second phase-change heat storage structure 52 is connected with the outlet of the membrane assembly 40 through the fourth water inlet pipe 14. The fifth water inlet pipe 15 is connected between the inlet of the first distillate tank 17 and the outlet of the first phase change heat storage structure 51, and the sixth water inlet pipe 16 is connected between the inlet of the first distillate tank 17 and the outlet of the second phase change heat storage structure 52. A first return line 61 is connected between the outlet of the first phase change heat storage structure 51 and the inlet of the heat exchanger assembly 30 and a second return line 62 is connected between the outlet of the second phase change heat storage structure 52 and the inlet of the heat exchanger assembly 30. The outlet pipe 63 is connected to the outlet of the first tank 17. Through the above arrangement, raw water enters the heat exchanger assembly 30 through the first water inlet pipe 11 and is heated in the heat exchanger assembly 30, the heated raw water forms steam and water, and the steam and water enter the membrane assembly 40, so that filtration is realized, and fresh water is generated. Fresh water continuously runs to the first phase-change heat storage structure 51, the first phase-change heat storage structure 51 absorbs heat in the fresh water, and finally the fresh water flows out through the water outlet pipe. The heat release of the first phase change heat storage structure 51 heats the heat exchanger assembly 30 through the first return line 61, which can reduce the energy consumption of the heat exchanger assembly 30. The first phase change heat storage structure 51 and the second phase change heat storage structure 52 are alternately used, that is, when the first phase change heat storage structure 51 releases heat, the second phase change heat storage structure 52 absorbs heat, and when the first phase change heat storage structure 51 absorbs heat, the second phase change heat storage structure 52 releases heat. This allows the first and second phase change heat storage structures 51 and 52 to heat the heat exchanger assembly 30, respectively, which allows the heat exchanger assembly 30 to be continuously heated, which eliminates the need for a separate heating device to heat the heat exchanger assembly 30. Therefore, the technical scheme effectively solves the problem that a large amount of coolant is needed in the membrane distillation process in the related technology, so that the energy consumption is overlarge.
In order to reduce the consumption of the coolant, the technical scheme of the embodiment is to recycle the latent heat of the steam by using the material with phase change because the phase change is generally higher, and is one of important ways to reduce the energy consumption of the membrane distillation process.
In the present embodiment, the interiors of the first phase-change heat storage structure 51 and the second phase-change heat storage structure 52 are filled with a heat storage material, specifically, in the present embodiment, paraffin is filled, but it is also possible to use coconut oil or the like.
As shown in fig. 1, in the present embodiment, the membrane distillation apparatus further includes: a second distillate tank 18, the inlet of the second distillate tank 18 being connected to the auxiliary outlet of the heat exchanger assembly 30; a seventh water inlet pipe 191 and an eighth water inlet pipe 192, the seventh water inlet pipe 191 being connected between the outlet of the second fraction tank 18 and the inlet of the first phase change heat storage structure 51, the eighth water inlet pipe 192 being connected between the outlet of the second fraction tank 18 and the inlet of the second phase change heat storage structure 52. The second tank 18 is connected to the outlet of the heat exchanger assembly 30 such that the second tank 18 is capable of storing hot water, which flows to the first and second phase change heat storage structures 51 and 52 through the seventh and eighth water inlet pipes 191 and 192, respectively, thereby heating the first and second phase change heat storage structures 51 and 52 such that the thermal efficiency of the first and second phase change heat storage structures 51 and 52 is higher. While the heat exchanger assembly 30 can be better heated, which can improve the efficiency of heating the heat exchanger assembly 30. Meanwhile, the raw water is directly transmitted to the first phase-change heat storage structure 51 and the second phase-change heat storage structure 52 after being heated by the heat exchanger assembly 30, so that the heat loss of the hot water is smaller, and further more heat is absorbed by the first phase-change heat storage structure 51 and the second phase-change heat storage structure 52.
Specifically, the first heat exchanger 31 is a shell-and-tube heater, and the hot water in the first heat exchanger 31 enters the second distillate tank 18, enters the first phase change heat storage structure 51 or the second phase change heat storage structure 52, and flows back to the first heat exchanger 31 through the first return line 61 or the second return line 62.
As shown in fig. 1, in the present embodiment, the heat exchanger assembly 30 includes a first heat exchanger 31 and a second heat exchanger 32, the first heat exchanger 31 and the second heat exchanger 32 are both connected to the first water inlet pipe 11, the second heat exchanger 32 is disposed between the first heat exchanger 31 and the feed liquid tank 20, an outlet of the first phase-change heat storage structure 51 is connected to an inlet of the first heat exchanger 31, an outlet of the second phase-change heat storage structure 52 is connected to an inlet of the first heat exchanger 31, and the membrane distillation apparatus further includes a steam generator 64, and the steam generator 64 is connected to the second heat exchanger 32. The arrangement of the first heat exchanger 31 and the second heat exchanger 32 can further improve the heating efficiency, specifically, the seventh water inlet pipe 191 is connected between the first phase change heat storage structure 51 and the second fraction tank 18, and the eighth water inlet pipe 192 is connected between the second phase change heat storage structure 52 and the second fraction tank 18, that is, the first phase change heat storage structure 51 and the second phase change heat storage structure 52 heat the first heat exchanger 31, and the steam generator is selectively turned on to determine whether to heat the second heat exchanger. At initial start-up, the steam generator 64 is started, raw water is heated at the second heat exchanger 32 and flows to the first phase change heat storage structure 51 and the second phase change heat storage structure 52, the first heat exchanger 31 is heated when the first phase change heat storage structure 51 and the second phase change heat storage structure 52 release heat, so that the raw water can be preheated, the temperature of the raw water is further increased under the action of the steam generator 64, and after the whole membrane distillation device circulates, the raw water can be heated only by the first phase change heat storage structure 51 and the second phase change heat storage structure 52 without starting the steam generator 64.
As shown in fig. 1, in the present embodiment, the membrane distillation apparatus further includes a first pump 65 and a third return line 66, a first end of the third return line 66 is connected to the feed liquid tank 20, a second end of the third return line 66 is connected to the inlet of the second heat exchanger 32, and the first pump 65 is connected to the third return line 66. The first pump 65 can pump the liquid in the feed liquid tank 20 into the second heat exchanger 32 again, so that the temperature of raw water can be further increased, and the effect of membrane distillation can be ensured.
In this embodiment, as shown in fig. 1, the membrane distillation apparatus further includes a fourth return line 67, a first end of the fourth return line 67 is connected to the inlet of the feed liquid tank 20, and a second end of the fourth return line 67 is connected to the outlet of the membrane module 40. The fourth return line 67 is provided to allow raw water not filtered by the membrane module 40 to flow into the feed liquid tank 20, and to be further transferred to the second heat exchanger 32 under the action of the feed liquid tank 20 and the first pump 65, thereby heating the raw water again, and improving the membrane distillation effect.
As shown in fig. 1, in the present embodiment, the second water inlet pipe 12 is provided with a second pump 121 and a filter 122, and the second pump 121 is provided between the filter 122 and the feed liquid tank 20. The above-described arrangement of the second pump 121 enables the flow of raw water, i.e., enables the raw water to flow to the membrane module 40. The filter 122 is provided to primarily perform filtration to filter impurities in raw water.
As shown in fig. 1, in the present embodiment, a first gas-liquid separator 151 is provided on the fifth water inlet pipe 15, and a second gas-liquid separator 161 is provided on the sixth water inlet pipe 16. The arrangement can split water and steam, the water is directly discharged, and the steam is discharged after being condensed.
As shown in fig. 1, in the present embodiment, the membrane distillation apparatus further includes a refrigeration apparatus 71 and a ninth water inlet pipe 72, a first end of the ninth water inlet pipe 72 is connected to both the outlet of the first gas-liquid separator 151 and the outlet of the second gas-liquid separator 161, a second end of the ninth water inlet pipe 72 is connected to the inlet of the first distillate tank 17, and the refrigeration apparatus 71 is connected to the ninth water inlet pipe 72. The cooling device 71 is provided to cool the steam, thereby condensing the steam.
As shown in fig. 1, in the present embodiment, the membrane distillation apparatus further includes a third pump 73, and the third pump 73 is connected to a ninth water inlet pipe 72 through a suction pipe 74. The third pump is a suction pump arranged to suck water from the water in the first and second phase change heat storage structures 51, 52 into the first distillate tank 17.
As shown in fig. 1, in the present embodiment, the membrane distillation apparatus further includes a third gas-liquid separator 75, and the third gas-liquid separator 75 is connected to the ninth water inlet pipe 72 and connected to the suction pipe 74. The third gas-liquid separator 75 can further achieve water vapor split.
The first heat exchanger 31, the second heat exchanger 32, and the upper portion of the refrigerating apparatus 71 are each provided with a purge valve for discharging non-condensable gas. A drain valve is provided below the second heat exchanger 32 to drain condensed water.
As shown in fig. 1, in the present embodiment, the membrane distillation apparatus further includes a first valve, a second valve, a third valve, a fourth valve, a fifth valve, a sixth valve, a seventh valve, an eighth valve, a ninth valve, a tenth valve, an eleventh valve, a twelfth valve, and a thirteenth valve. The first water inlet pipe 11 is provided with a first valve, the first valve is located between a water inlet of the first water inlet pipe 11 and the first heat exchanger 31, the second valve is arranged on the third return pipeline 66, the second water inlet pipe 12 is provided with a third valve, the shared section of the third water inlet pipe 13 and the fourth water inlet pipe 14 is provided with a fourth valve, the third water inlet pipe 13 is provided with an eleventh valve, the fourth water inlet pipe 14 is provided with a fifth valve, the seventh water inlet pipe 191 is provided with a tenth valve, the eighth water inlet pipe 192 is provided with a ninth valve, the shared section of the first return pipeline 61 and the second return pipeline 62 is provided with an eighth valve, the first return pipeline 61 is provided with a thirteenth valve, the second return pipeline 62 is provided with a seventh valve, the fifth water inlet pipe 15 is provided with a twelfth valve, and the sixth water inlet pipe 16 is provided with a sixth valve. A first flow meter is provided between the steam generator 64 and the second heat exchanger 32, a second flow meter is provided on the third return line 66, and a third flow meter is provided on the second inlet pipe 12.
As shown in fig. 1, the membrane distillation apparatus of this embodiment operates as follows:
raw water enters the first heat exchanger 31 after the flow rate of the raw water is regulated by the first valve from the first water inlet pipe 11, is preheated, is further heated at the second heat exchanger 32, and enters the feed liquid tank 20 to serve as hot-side feed liquid of membrane distillation. The vapor which permeates through the membrane is pumped into the first phase change heat storage structure 51 through the third pump 73 to exchange heat with the phase change heat storage material and then condensate, the condensate water which passes through the first gas-liquid separator 151 enters the first distillate tank 17, the uncondensed vapor continues to be condensed through the refrigerating device, and the condensate water also enters the first distillate tank 17. Very little non-condensable gases and water vapor are vented to atmosphere by third pump 73. At this time, the fourth valve, the fifth valve and the sixth valve are opened, and the seventh valve is closed. In the process that raw water continuously enters the system, the feed tank 20 continuously discharges concentrated water through a discharge port on the feed tank 20, and the first distillate tank 17 also continuously discharges fresh water through the water outlet pipe 63. During the heat storage of the first phase-change heat storage structure 51, the second phase-change heat storage structure 52 releases heat, and as a preheating heat source for raw water, the tenth valve, the eighth valve, and the thirteenth valve are opened, and the eleventh valve and the twelfth valve are closed. During the heat storage process of the second phase-change heat storage structure 52, the first phase-change heat storage structure 51 releases heat, and as a preheating heat source of raw water, the fourth valve, the eleventh valve and the twelfth valve are opened, and the tenth valve and the thirteenth valve are closed. The opening and closing of the valves are interlocked, so that automatic control is realized.
As shown in fig. 1, in the present embodiment,
the heat storage process is as follows: when the steam passing through the membrane module 40 is pumped to the inlet of the first phase-change heat storage structure 51 by the third pump 73, after exchanging heat with the first phase-change heat storage structure 51, part of the steam is condensed, after passing through the first gas-liquid separator 151, the condensed water enters the first distillate tank 17, the uncondensed steam continues to be condensed after entering the refrigerating device 71, the gas-liquid mixture passes through the third gas-liquid separator 75, the condensed water enters the first distillate tank 17, and a small amount of uncondensed steam is pumped away by the third pump 73. And until the phase change material in the first phase change heat storage structure 51 reaches the expected temperature, the heat storage process of the first phase change heat storage structure 51 is ended, and the heat release process is waited. While the heat storage process of the second phase change heat storage structure 52 is turned on.
Exothermic process: when the phase change unit in the first phase change heat storage structure 51 reaches the set temperature, the first valve is opened, cold wastewater enters the first heat exchanger 31 to exchange heat with the first phase change heat storage structure 51, namely, the first phase change heat storage structure 51 flows back to the first heat exchanger 31 through the first return pipeline 61, and the feed liquid enters the second heat exchanger 32 after being heated and is further heated by the steam generator 64. The heat release process of the first phase change heat storage structure 51 is ended and the next heat storage process is waited. The first phase-change heat storage structure 51 and the second phase-change heat storage structure 52 alternately store and release heat, serving as both a preheater for raw water and a condenser for permeated film steam.
The preheating and heating process of raw water: raw water is preheated from the first water inlet pipe 11 through the first heat exchanger 31, is further heated by the second heat exchanger 32 and then enters the feed liquid tank 20 to be used as hot-side feed liquid for membrane distillation. The heating medium of the first heat exchanger 31 is fresh water of the second distillate tank 18, the heat source is derived from the first phase-change heat storage structure 51 and the second phase-change heat storage structure 52, and the preheating of the raw water is also an exothermic process of the first phase-change heat storage structure 51 and the second phase-change heat storage structure 52. The heating medium of the second heat exchanger 32 is water vapor generated by the vapor generator 64.
Membrane distillation process: the heated raw water in the feed liquid tank 20 enters the membrane module 40 under the drive of the second pump 121, circulates in a loop formed by the membrane module 40 and the feed liquid tank 20, volatilizes water in the raw water, permeates the membrane module 40 under the pushing of the water vapor partial pressure difference and the pressure difference caused by the third pump 73, and enters the permeation side of the membrane module 40 to realize the separation of water and salt.
Specifically, in the present embodiment, raw water passing through the first phase-change heat storage structure 51 and the second phase-change heat storage structure 52 can enter the inside of the first heat exchanger 31 and also can enter the heat exchange line of the first heat exchanger 31, respectively.
In the description of the present invention, it should be understood that the azimuth or positional relationships indicated by the azimuth terms such as "front, rear, upper, lower, left, right", "lateral, vertical, horizontal", and "top, bottom", etc., are generally based on the azimuth or positional relationships shown in the drawings, merely to facilitate description of the present invention and simplify the description, and these azimuth terms do not indicate and imply that the apparatus or elements referred to must have a specific azimuth or be constructed and operated in a specific azimuth, and thus should not be construed as limiting the scope of protection of the present invention; the orientation word "inner and outer" refers to inner and outer relative to the contour of the respective component itself.
Spatially relative terms, such as "above … …," "above … …," "upper surface at … …," "above," and the like, may be used herein for ease of description to describe one device or feature's spatial location relative to another device or feature as illustrated in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations in use or operation in addition to the orientation depicted in the figures. For example, if the device in the figures is turned over, elements described as "above" or "over" other devices or structures would then be oriented "below" or "beneath" the other devices or structures. Thus, the exemplary term "above … …" may include both orientations of "above … …" and "below … …". The device may also be positioned in other different ways (rotated 90 degrees or at other orientations) and the spatially relative descriptors used herein interpreted accordingly.
In addition, the terms "first", "second", etc. are used to define the components, and are only for convenience of distinguishing the corresponding components, and the terms have no special meaning unless otherwise stated, and therefore should not be construed as limiting the scope of the present invention.
The above description is only of the preferred embodiments of the present invention and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A membrane distillation apparatus, comprising:
a first inlet pipe (11);
the inlet of the feed liquid tank (20) is connected with the first water inlet pipe (11);
the heat exchanger assembly (30), the inlet and the main outlet of the heat exchanger assembly (30) are connected to the first water inlet pipe (11);
the inlet of the membrane assembly (40) is connected with the outlet of the feed liquid tank (20) through a second water inlet pipe (12);
the inlet of the first phase-change heat storage structure (51) is connected with the outlet of the membrane assembly (40) through a third water inlet pipe (13);
the inlet of the second phase-change heat storage structure (52) is connected with the outlet of the membrane assembly (40) through a fourth water inlet pipe (14);
a fifth water inlet pipe (15), a sixth water inlet pipe (16) and a first fraction tank (17), wherein the fifth water inlet pipe (15) is connected between an inlet of the first fraction tank (17) and an outlet of the first phase change heat storage structure (51), and the sixth water inlet pipe (16) is connected between an inlet of the first fraction tank (17) and an outlet of the second phase change heat storage structure (52);
a first return line (61) and a second return line (62), the first return line (61) being connected between the outlet of the first phase change heat storage structure (51) and the inlet of the heat exchanger assembly (30), the second return line (62) being connected between the outlet of the second phase change heat storage structure (52) and the inlet of the heat exchanger assembly (30);
a water outlet pipe (63) connected with the outlet of the first fraction tank (17);
the first phase-change heat storage structure (51) and the second phase-change heat storage structure (52) are alternately used, when the first phase-change heat storage structure (51) releases heat, the second phase-change heat storage structure (52) absorbs heat, and when the first phase-change heat storage structure (51) absorbs heat, the second phase-change heat storage structure (52) releases heat.
2. The membrane distillation apparatus of claim 1, further comprising:
a second distillate tank (18), an inlet of the second distillate tank (18) being connected to an auxiliary outlet of the heat exchanger assembly (30);
a seventh water inlet pipe (191) and an eighth water inlet pipe (192), wherein the seventh water inlet pipe (191) is connected between the outlet of the second fraction tank (18) and the inlet of the first phase-change heat storage structure (51), and the eighth water inlet pipe (192) is connected between the outlet of the second fraction tank (18) and the inlet of the second phase-change heat storage structure (52).
3. Membrane distillation device according to claim 1, wherein the heat exchanger assembly (30) comprises a first heat exchanger (31) and a second heat exchanger (32), the first heat exchanger (31) and the second heat exchanger (32) are both connected to the first water inlet pipe (11), the second heat exchanger (32) is arranged between the first heat exchanger (31) and the feed liquid tank (20), the outlet of the first phase change heat storage structure (51) is connected to the inlet of the first heat exchanger (31), the outlet of the second phase change heat storage structure (52) is connected to the inlet of the first heat exchanger (31), the membrane distillation device further comprises a steam generator (64), and the steam generator (64) is connected to the second heat exchanger (32).
4. A membrane distillation apparatus according to claim 3, further comprising a first pump (65) and a third return line (66), a first end of the third return line (66) being connected to the feed liquid tank (20), a second end of the third return line (66) being connected to the inlet of the second heat exchanger (32), the first pump (65) being connected to the third return line (66).
5. Membrane distillation device according to any one of claims 1 to 4, further comprising a fourth return line (67), a first end of the fourth return line (67) being connected to the inlet of the feed liquid tank (20), a second end of the fourth return line (67) being connected to the outlet of the membrane module (40).
6. Membrane distillation device according to any one of claims 1 to 4, wherein a second pump (121) and a filter (122) are provided on the second water inlet pipe (12), the second pump (121) being provided between the filter (122) and the feed liquid tank (20).
7. Membrane distillation device according to any one of claims 1 to 4, wherein the fifth water inlet pipe (15) is provided with a first gas-liquid separator (151) and the sixth water inlet pipe (16) is provided with a second gas-liquid separator (161).
8. The membrane distillation apparatus according to claim 7, further comprising a refrigeration device (71) and a ninth water inlet pipe (72), a first end of the ninth water inlet pipe (72) being connected to both the outlet of the first gas-liquid separator (151) and the outlet of the second gas-liquid separator (161), a second end of the ninth water inlet pipe (72) being connected to the inlet of the first distillate tank (17), the refrigeration device (71) being connected to the ninth water inlet pipe (72).
9. Membrane distillation device according to claim 8, further comprising a third pump (73), the third pump (73) being connected to the ninth water inlet pipe (72) by a suction pipe (74).
10. Membrane distillation device according to claim 9, further comprising a third gas-liquid separator (75), the third gas-liquid separator (75) being connected to the ninth water inlet pipe (72) and to the suction pipe (74).
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