CN110404411B - Membrane distillation system and method with waste heat recovery coupling MVR - Google Patents
Membrane distillation system and method with waste heat recovery coupling MVR Download PDFInfo
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- CN110404411B CN110404411B CN201910658991.5A CN201910658991A CN110404411B CN 110404411 B CN110404411 B CN 110404411B CN 201910658991 A CN201910658991 A CN 201910658991A CN 110404411 B CN110404411 B CN 110404411B
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- 239000012528 membrane Substances 0.000 title claims abstract description 155
- 238000004821 distillation Methods 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 39
- 239000002918 waste heat Substances 0.000 title claims abstract description 19
- 238000011084 recovery Methods 0.000 title claims abstract description 17
- 230000008878 coupling Effects 0.000 title claims abstract description 16
- 238000010168 coupling process Methods 0.000 title claims abstract description 16
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 16
- 239000007788 liquid Substances 0.000 claims abstract description 235
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 104
- 239000000463 material Substances 0.000 claims abstract description 28
- 239000003507 refrigerant Substances 0.000 claims description 17
- 238000001514 detection method Methods 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 238000005485 electric heating Methods 0.000 description 13
- 238000005265 energy consumption Methods 0.000 description 11
- 239000000243 solution Substances 0.000 description 11
- 238000004891 communication Methods 0.000 description 9
- 239000012510 hollow fiber Substances 0.000 description 8
- 230000008569 process Effects 0.000 description 7
- 238000000926 separation method Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 230000002209 hydrophobic effect Effects 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000012982 microporous membrane Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- -1 polytetrafluoroethylene Polymers 0.000 description 1
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 1
- 239000004810 polytetrafluoroethylene Substances 0.000 description 1
- 230000003252 repetitive effect Effects 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 239000011555 saturated liquid Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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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
- 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
- B01D61/368—Accessories; Auxiliary operations
-
- 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
- C02F1/008—Control or steering systems not provided for elsewhere in subclass C02F
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24H—FLUID HEATERS, e.g. WATER OR AIR HEATERS, HAVING HEAT-GENERATING MEANS, e.g. HEAT PUMPS, IN GENERAL
- F24H4/00—Fluid heaters characterised by the use of heat pumps
- F24H4/02—Water heaters
- F24H4/04—Storage heaters
-
- G—PHYSICS
- G05—CONTROLLING; REGULATING
- G05D—SYSTEMS FOR CONTROLLING OR REGULATING NON-ELECTRIC VARIABLES
- G05D27/00—Simultaneous control of variables covered by two or more of main groups G05D1/00 - G05D25/00
- G05D27/02—Simultaneous control of variables covered by two or more of main groups G05D1/00 - G05D25/00 characterised by the use of electric means
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- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- General Physics & Mathematics (AREA)
- Automation & Control Theory (AREA)
- Thermal Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
A membrane distillation system with a waste heat recovery coupling MVR and a control method thereof comprise a material liquid tank, a condenser, a water tank, an evaporator, a first compressor and a throttling device; a membrane module, a circulating pump and a heat exchanger; a second compressor; an evaporator is arranged in the water tank, a condenser is arranged in the material liquid tank, and the evaporator, the compressor, the condenser and the throttling device form a first loop; the material liquid tank, the membrane component and the heat exchanger form a second loop; the circulating pump is used for providing power for the second loop; the steam outlet of the membrane component is communicated with the inlet of the second compressor, the outlet of the second compressor is communicated with the first inlet of the heat exchanger, and the first outlet of the heat exchanger is communicated with the first inlet of the water tank. According to the invention, waste heat recovery is introduced into the membrane distillation system coupled with MVR, and the cascade application of energy in the membrane distillation system is realized by recovering the waste heat, so that the energy utilization rate is improved, and the production cost is reduced.
Description
Technical Field
The invention relates to a membrane distillation system and a method, in particular to a membrane distillation system and a method with a waste heat recovery coupling MVR.
Background
The membrane separation technology is based on the selective permeability of a high molecular hydrophobic microporous membrane, and a differential pressure driving force is formed in the wall surface and the membrane cavity of the membrane, so that water in the solution permeates the membrane pores in the form of water molecules, and the separation of solute solvents is realized. Because of the characteristics of high treatment efficiency, wide application range, easy coupling with other technologies and the like, the method has been widely applied in the field of concentration. Compared with the traditional multi-effect evaporation, mechanical vapor recompression and multi-stage flash evaporation technologies, the membrane distillation technology has great advantages in the aspects of purity of separated water, strong acid and alkali resistance, simplicity in operation and the like. However, most of the water vapor is directly condensed in terms of water vapor treatment, and the latent heat of the water vapor is not recovered, so that the energy consumption is high. Thus, existing membrane distillation techniques are often used in combination with other techniques to reduce system energy consumption, where coupling with Mechanical Vapor Recompression (MVR) techniques has been widely studied.
Chinese patent CN108744980a discloses a system and method for concentrating highly corrosive solution without liquid storage membrane assembly coupling MVR, the system comprises a raw material tank, an electric heating device, a pressure-reducing membrane assembly, a membrane separator, etc. The system separates out water vapor through the decompression membrane component under the negative pressure environment, and heats the concentrated solution after enthalpy increase through the compressor, so as to recover latent heat in secondary steam and improve the energy utilization rate. However, in the system, electric heating is adopted for preheating raw materials and maintaining the constant temperature of feed liquid, so that higher energy consumption is caused; the secondary steam is condensed into condensed water which directly flows into a condensate pipe for natural cooling, and the waste heat is not recycled; the selected compressor is not associated with the temperature of the feed liquid in real time, frequency modulation is required to be controlled manually in actual operation, and the system is unstable in operation.
Chinese patent No. CN103080013B discloses a vapor compression membrane distillation desalination device in which the latent heat of condensation generated by the temperature gradient across the membrane distillation module is transferred directly to the latent heat of vaporization during desalination of a liquid fluid stream, the device comprising an MD module, a vapor compressor, etc. The system realizes recycling of the secondary steam, however, the system only discusses application in salt solution, cannot be applied to a strongly corrosive solution, and sensible heat in condensate is not recycled.
Chinese patent CN206199023U discloses a membrane distillation apparatus with vapor mechanical compression, in which the system improves the enthalpy of secondary vapor by a compressor for heating the concentrate, recovers the latent heat of secondary vapor, and improves the energy utilization rate. The system also adopts electric heating to preheat the feed liquid, so that the energy consumption is higher; the constant temperature of the feed liquid of the system is controlled by the combined action of the electric heating and the compressor, so that the complexity of the system operation is increased; the system has insufficient purity for steam separation, so that the system cannot be applied to evaporation concentration of a highly corrosive solution; the selected compressor is not associated with the temperature of the feed liquid in real time, frequency modulation is required to be controlled manually in actual operation, and the system is unstable in operation.
Chinese patent CN208678828U discloses a membrane distillation coupling MVR concentrated strong corrosion solution system, which enters a membrane separator from the top outlet of a membrane tube to separate and purify, then enters a vapor compressor to heat up and pressurize, and the compressed vapor enters a heat exchanger to release latent heat to the concentrated solution from the upper outlet of a membrane assembly, and finally is condensed into saturated liquid water to enter a condensate tank to be collected. The system recovers the latent heat of the secondary steam, improves the energy utilization rate, and applies the membrane distillation system to the solution with strong corrosiveness. However, the system still does not solve the problems of high energy consumption caused by adopting electric heating to keep the temperature of the feed liquid constant and energy waste caused by recycling of the waste heat of the condensed water.
In summary, in the combination process of the existing membrane distillation system and the mechanical vapor compression system, the vapor separated from the membrane is compressed and enthalpy-increased by the compressor, and then the concentrated feed liquid is heated, so that the secondary latent heat of the vapor is recovered. However, electric heating is adopted in the preheating process of the feed liquid, and continuous operation is required for maintaining the constant temperature of the feed liquid; the secondary steam is condensed directly in the atmosphere after being condensed, and part of sensible heat is not utilized; most of the selected compressors are fixed-frequency compressors, and no connection can be established through a temperature sensor in the feed liquid. The energy consumption in the membrane distillation process is increased, the production cost is increased, and the running stability of the system is reduced.
In summary, the membrane distillation system and method for coupling MVR in the prior art have the following technical problems: 1) In the preheating process of the feed liquid, electric heating is adopted to heat, and after the system stably operates, the electric heating needs to continuously operate in order to maintain the temperature of the feed liquid constant. 2) The secondary steam is condensed directly in the atmosphere after being condensed, and the sensible heat of the condensed water is not utilized. 3) The compressor is mostly controlled at fixed frequency, and the connection between the temperature sensor in the feed liquid and the temperature of the feed liquid is not established, so that the complexity of subsequent operation is increased.
Disclosure of Invention
In view of the above, the invention provides a membrane distillation system with a waste heat recovery coupling MVR and a method thereof, wherein the waste heat recovery is introduced into the membrane distillation system with the coupling MVR, and the gradient application of energy in the membrane distillation system is realized by recovering sensible heat of condensed water, so that the energy utilization rate is improved, and the production cost is reduced.
Specifically:
The utility model provides a take waste heat recovery coupling MVR's membrane distillation system, includes feed liquid jar, condenser, water tank, evaporimeter, first compressor, throttling arrangement, membrane module, circulating pump, heat exchanger, second compressor, vacuum pump:
An evaporator is arranged in the water tank, a condenser is arranged in the material liquid tank, and the evaporator, the first compressor, the condenser and the throttling device form a first loop; the method comprises the following steps: the outlet of the evaporator is communicated with the inlet of the first compressor, the outlet of the first compressor is communicated with the inlet of the condenser, the outlet of the condenser is communicated with the inlet of the throttling device, and the outlet of the throttling device is communicated with the inlet of the evaporator;
the material liquid tank, the membrane component and the heat exchanger form a second loop; the method comprises the following steps: the feed liquid outlet of the feed liquid tank is communicated with the feed liquid inlet of the membrane assembly, the feed liquid outlet of the membrane assembly is communicated with the feed liquid inlet of the heat exchanger, and the feed liquid outlet of the heat exchanger is communicated with the feed liquid inlet of the feed liquid tank; the second loop is also provided with a circulating pump, and the circulating pump is used for providing power for the second loop;
The steam outlet of the membrane component is communicated with the inlet of the second compressor, the outlet of the second compressor is communicated with the first inlet of the heat exchanger, and the first outlet of the heat exchanger is communicated with the first inlet of the water tank;
the vacuum pump is in communication with the vapor outlet of the membrane module.
Preferably, the vapor outlet of the membrane assembly is in communication with the inlet of the second compressor after passing through the vapor-liquid separator.
Preferably, the device further comprises a vacuum material tank, wherein the vacuum pump is communicated with an outlet of the vacuum material tank, and an inlet of the vacuum material tank is communicated with an inlet or an outlet of the gas-liquid separator through a fourth control valve.
Preferably, the vacuum pump is connected with the outlet of the vacuum tank, and the inlet of the vacuum tank is connected between the second compressor and the fifth control valve through the fourth control valve.
Preferably, the water tank further comprises an air inlet and an air outlet, the sixth control valve is arranged at the air inlet of the water tank, and the seventh control valve is arranged at the air outlet of the water tank.
Preferably, the air conditioner further comprises a fan, wherein the fan is used for accelerating the circulation of air in the water tank.
Preferably, a first control valve is formed between the second loop feeding liquid tank and the membrane component, and a second control valve is formed between the second loop upper heat exchanger and the feed liquid tank.
Preferably, a third control valve is provided between the first outlet of the heat exchanger and the first inlet of the water tank.
Preferably, a fifth control valve is provided between the outlet of the second compressor and the first inlet of the heat exchanger.
Preferably, a liquid level sensor is arranged in the water tank, and the liquid level sensor is positioned at a preset height from the bottom of the water tank.
Preferably, a temperature sensor for measuring the temperature of the feed liquid is arranged in the feed liquid tank.
Preferably, at least one of the first compressor and the second compressor is a variable frequency compressor.
In addition, the invention also provides a control method of the membrane distillation system, a liquid level sensor is arranged in a water tank of the membrane distillation system, the liquid level sensor is positioned at a preset height from the bottom of the water tank, and the control method comprises the following steps:
S01: acquiring a detection result of a liquid level sensor;
S02: when the liquid level is not detected, controlling the membrane distillation system to operate according to a first operation mode; when the liquid level is detected, the membrane distillation system is controlled to operate in a second mode of operation.
Preferably, a first control valve is formed between a second loop feeding liquid tank and a membrane component of the membrane distillation system, and a second control valve is formed between a second loop heat exchanger and a feed liquid tank; a third control valve is arranged between the first outlet of the heat exchanger and the first inlet of the water tank; the steam outlet of the membrane component is communicated with the inlet of the second compressor through the gas-liquid separator, the vacuum pump is communicated with the outlet of the vacuum charging bucket, and the inlet of the vacuum charging bucket is communicated with the inlet or the outlet of the gas-liquid separator through the fourth control valve; a fifth control valve is arranged between the outlet of the second compressor and the first inlet of the heat exchanger; the air inlet of the water tank is provided with a sixth control valve, and the air outlet of the water tank is provided with a seventh control valve;
The first operation mode comprises the following steps: SA1, a sixth control valve and a seventh control valve are opened, the first control valve to the fifth control valve are closed, the first compressor starts to operate, and heat of the refrigerant on the first loop is transferred to feed liquid in the feed liquid tank through the operation of the first compressor;
SA2, acquiring the temperature of the feed liquid detected by a temperature sensor;
SA3, when the temperature of the feed liquid reaches a first preset temperature, a fourth control valve is opened, the vacuum pump starts to operate, and when the steam outlet of the membrane assembly reaches a preset pressure, the fourth control valve is closed; opening the first, second, third and fifth control valves, and starting the circulating pump to operate, wherein the circulating pump drives the feed liquid to circularly flow in the second loop; the second compressor starts to operate, compresses the vapor flowing out of the gas-liquid separator, flows through the heat exchanger, and returns to the water tank.
Preferably, a first control valve is formed between a second loop feeding liquid tank and a membrane component of the membrane distillation system, and a second control valve is formed between a second loop heat exchanger and a feed liquid tank; a third control valve is arranged between the first outlet of the heat exchanger and the first inlet of the water tank; the steam outlet of the membrane component is communicated with the inlet of the second compressor through the gas-liquid separator, the vacuum pump is communicated with the outlet of the vacuum charging bucket, and the inlet of the vacuum charging bucket is communicated with the inlet or the outlet of the gas-liquid separator through the fourth control valve; a fifth control valve is arranged between the outlet of the second compressor and the first inlet of the heat exchanger; the air inlet of the water tank is provided with a sixth control valve, and the air outlet of the water tank is provided with a seventh control valve;
The second mode of operation includes the steps of: SC1: the sixth control valve and the seventh control valve are closed, the first control valve, the second control valve, the third control valve and the fifth control valve are opened, and the fourth control valve is closed; the first compressor is operated, and heat of the refrigerant on the first loop is transferred to feed liquid of the feed liquid tank through the operation of the first compressor;
SC2: the circulating pump operates and drives the feed liquid to circularly flow in the second loop; the second compressor is operated, and the second compressor compresses the vapor flowing out of the gas-liquid separator, flows through the heat exchanger and returns to the water tank.
Preferably, a temperature sensor for measuring the temperature of the feed liquid is arranged in the feed liquid tank, the first compressor and the second compressor are variable frequency compressors, and the step S02 further comprises the following step S03: the first compressor and the second compressor are controlled to operate at different frequencies respectively according to the measured value of the temperature sensor.
According to the invention, waste heat recovery is introduced into the membrane distillation system coupled with MVR, and the cascade application of energy in the membrane distillation system is realized by recovering the waste heat, so that the energy utilization rate is improved, and the production cost is reduced.
It is to be understood that both the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive of the disclosure.
Drawings
The above and other objects, features and advantages of the present disclosure will become more apparent by describing in detail exemplary embodiments thereof with reference to the attached drawings. The drawings described below are merely examples of the present disclosure and other drawings may be obtained from these drawings without inventive effort for a person of ordinary skill in the art.
FIG. 1 is a schematic diagram of a membrane distillation system with heat recovery coupled MVR of the present invention.
Wherein: 1a material liquid tank, 2a condenser, 3a circulating pump, 4-1 a first control valve, 4-2 a second control valve, 4-3 a third control valve, 4-4 a fourth control valve, 4-5 a fifth control valve, 4-6 a sixth control valve, 4-7 a seventh control valve, 5a membrane module, 6 a hollow fiber membrane tube, 7a membrane cavity, 8 a gas-liquid separator, 9a heat exchanger, 10a water tank, 11 an evaporator, 12a throttling device, 13 a first compressor, 14 a second compressor, 15 a vacuum tank, 16 a vacuum pump, 17a fan, 18 a liquid level sensor and 19 a temperature sensor.
Detailed Description
Example embodiments will now be described more fully with reference to the accompanying drawings. However, the exemplary embodiments can be embodied in many forms and should not be construed as limited to the embodiments set forth herein; rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the concept of the example embodiments to those skilled in the art. The same reference numerals in the drawings denote the same or similar parts, and thus a repetitive description thereof will be omitted.
Furthermore, the described features, structures, or characteristics may be combined in any suitable manner in one or more embodiments. In the following description, numerous specific details are provided to give a thorough understanding of embodiments of the disclosure. One skilled in the relevant art will recognize, however, that the disclosed aspects may be practiced without one or more of the specific details, or with other methods, components, devices, steps, etc. In other instances, well-known methods, devices, implementations, or operations are not shown or described in detail to avoid obscuring aspects of the disclosure.
The block diagrams depicted in the figures are merely functional entities and do not necessarily correspond to physically separate entities. That is, the functional entities may be implemented in software, or in one or more hardware modules or integrated circuits, or in different networks and/or processor devices and/or microcontroller devices.
The flow diagrams depicted in the figures are exemplary only, and do not necessarily include all of the elements and operations/steps, nor must they be performed in the order described. For example, some operations/steps may be decomposed, and some operations/steps may be combined or partially combined, so that the order of actual execution may be changed according to actual situations.
It will be understood that, although the terms first, second, third, etc. may be used herein to describe various structures, these structures should not be limited by these terms. These terms are used to distinguish one structure from another structure. Thus, a first structure discussed below may be referred to as a second structure without departing from the teachings of the disclosed concepts. As used herein, the term "and/or" includes any one of the associated listed items and all combinations of one or more.
Those skilled in the art will appreciate that the drawings are schematic representations of example embodiments and that the modules or flows in the drawings are not necessarily required to practice the present disclosure, and therefore, should not be taken to limit the scope of the present disclosure.
The following describes the details of the embodiment of the present invention with reference to fig. 1:
The utility model provides a take waste heat recovery coupling MVR's membrane distillation system, includes feed liquid jar 1, condenser 2, water tank 10, evaporimeter 11, first compressor 13, throttling arrangement 12, membrane module 5, circulating pump 3, heat exchanger 9, second compressor 14, vacuum pump 16:
An evaporator 11 is arranged in the water tank 10, and a condenser 2 is arranged in the feed liquid tank 1, wherein the evaporator 11, a first compressor 13, the condenser 2 and a throttling device 12 form a first loop; the method comprises the following steps: the outlet of the evaporator 11 is communicated with the inlet of the first compressor 13, the outlet of the first compressor 13 is communicated with the inlet of the condenser 2, the outlet of the condenser 2 is communicated with the inlet of the throttling device 12, and the outlet of the throttling device 12 is communicated with the inlet of the evaporator 11;
the material liquid tank 1, the membrane component 5 and the heat exchanger 9 form a second loop; the method comprises the following steps: the feed liquid outlet of the feed liquid tank 1 is communicated with the feed liquid inlet of the membrane assembly 5, the feed liquid outlet of the membrane assembly 5 is communicated with the feed liquid inlet of the heat exchanger 9, and the feed liquid outlet of the heat exchanger 9 is communicated with the feed liquid inlet of the feed liquid tank 1; the second loop is also provided with a circulating pump 3, and the circulating pump 3 is used for providing power for the second loop;
The steam outlet of the membrane component 5 is communicated with the inlet of the second compressor 14, the outlet of the second compressor 14 is communicated with the first inlet of the heat exchanger 9, and the first outlet of the heat exchanger 9 is communicated with the first inlet of the water tank 10;
Preferably, the vacuum pump 16 is in communication with the vapor outlet of the membrane module 5.
Wherein the communication may be direct communication or indirect communication, such as the vacuum pump 16 may be through communication with other components of the membrane module 5 that are in communication with the vapor outlet, such as the inlet and outlet of the vapor-liquid separator 8. The vacuum pump 16 is used to bring the vapor outlet of the membrane module 5 to a predetermined pressure so that the vapor can be separated out of the membranes in the membrane module 5.
Preferably, the vapor outlet of the membrane module 5 is in communication with the inlet of the second compressor 14 via the vapor-liquid separator 8.
Preferably, the vacuum separator further comprises a vacuum material tank 15, a vacuum pump 16 is communicated with an outlet of the vacuum material tank 15, and an inlet of the vacuum material tank 15 is communicated with an inlet or an outlet of the gas-liquid separator 8 through a fourth control valve 4-4.
Preferably, the vacuum tank 15 is further included, the vacuum pump 16 is communicated with an outlet of the vacuum tank 15, and an inlet of the vacuum tank 15 is connected between the second compressor 14 and the fifth control valve 4-5 through the fourth control valve 4-4.
Preferably, the water tank 10 further comprises an air inlet and an air outlet, the sixth control valve 4-6 is arranged at the air inlet of the water tank 10, and the seventh control valve 4-7 is arranged at the air outlet of the water tank 10.
Preferably, a fan 17 is also included, the fan 17 being used to accelerate the circulation of air in the tank 10.
Preferably, a first control valve 4-1 is formed between the second loop feeding liquid tank 1 and the membrane component 5, and a second control valve 4-2 is formed between the second loop upper heat exchanger 9 and the feed liquid tank 1.
Preferably, a third control valve 4-3 is provided between the first outlet of the heat exchanger 9 and the first inlet of the tank 10.
Preferably, a fifth control valve 4-5 is provided between the outlet of the second compressor 14 and the first inlet of the heat exchanger 9.
Preferably, a level sensor 18 is provided within the tank 10, the level sensor 18 being located at a predetermined height from the bottom of the tank 10.
Preferably, a temperature sensor 19 for measuring the temperature of the feed liquid is provided in the feed liquid tank 1.
Preferably, at least one of the first compressor 13 and the second compressor 14 is a variable frequency compressor.
In addition, the invention also provides a control method of the membrane distillation system, a liquid level sensor 18 is arranged in the water tank 10 of the membrane distillation system, the liquid level sensor 18 is positioned at a preset height from the bottom of the water tank 10, and the control method comprises the following steps:
S01: acquiring a detection result of the liquid level sensor 18;
S02: when the liquid level is not detected, controlling the membrane distillation system to operate according to a first operation mode; when the liquid level is detected, the membrane distillation system is controlled to operate in a second mode of operation.
Preferably, a first control valve 4-1 is formed between the second loop feeding liquid tank 1 and the membrane component 5 of the membrane distillation system, and a second control valve 4-2 is formed between the second loop upper heat exchanger 9 and the feed liquid tank 1; a third control valve 4-3 is arranged between the first outlet of the heat exchanger 9 and the first inlet of the water tank 10; the steam outlet of the membrane component 5 is communicated with the inlet of the second compressor 14 through the gas-liquid separator 8, the vacuum pump 16 is communicated with the outlet of the vacuum charging bucket 15, and the inlet of the vacuum charging bucket 15 is communicated with the inlet or outlet of the gas-liquid separator 8 through the fourth control valve 4-4; a fifth control valve 4-5 is arranged between the outlet of the second compressor 14 and the first inlet of the heat exchanger 9; the air inlet of the water tank 10 is provided with a sixth control valve 4-6, and the air outlet of the water tank 10 is provided with a seventh control valve 4-7;
The first operation mode comprises the following steps: SA1, the sixth control valve 4-6 and the seventh control valve 4-7 are opened, the first control valve 4-1, the second control valve 4-2, the third control valve 4-3, the fourth control valve 4-4 and the fourth control valve 4-5 are closed, the first compressor 13 starts to operate, and the heat of the refrigerant on the first loop is transferred to the feed liquid of the feed liquid tank 1 through the operation of the first compressor 13;
SA2, acquiring the temperature of the feed liquid detected by the temperature sensor 19;
SA3, when the temperature of the feed liquid reaches a first preset temperature, opening the fourth control valve 4-4, starting the vacuum pump 16 to operate, and when the steam outlet of the membrane assembly 5 reaches a preset pressure, closing the fourth control valve 4-4; opening the first, second, third and fifth control valves 4-1,4-2,4-3,4-5, starting the circulation pump 3, and driving the feed liquid to circularly flow in the second loop by the circulation pump 3; the second compressor 14 starts to operate, and the second compressor 14 compresses the vapor flowing out of the gas-liquid separator 8, flows through the heat exchanger 9, and returns to the water tank 10.
Preferably, a first control valve 4-1 is formed between the second loop feeding liquid tank 1 and the membrane component 5 of the membrane distillation system, and a second control valve 4-2 is formed between the second loop upper heat exchanger 9 and the feed liquid tank 1; a third control valve 4-3 is arranged between the first outlet of the heat exchanger 9 and the first inlet of the water tank 10; the steam outlet of the membrane component 5 is communicated with the inlet of the second compressor 14 through the gas-liquid separator 8, the vacuum pump 16 is communicated with the outlet of the vacuum charging bucket 15, and the inlet of the vacuum charging bucket 15 is communicated with the inlet or outlet of the gas-liquid separator 8 through the fourth control valve 4-4; a fifth control valve 4-5 is arranged between the outlet of the second compressor 14 and the first inlet of the heat exchanger 9; the air inlet of the water tank 10 is provided with a sixth control valve 4-6, and the air outlet of the water tank 10 is provided with a seventh control valve 4-7;
The second mode of operation includes the steps of: SC1: the sixth control valve 4-6,4-7 is closed, the first control valve 4-1, the second control valve 4-2, the third control valve 4-3, the fifth control valve 4-5 is opened, and the fourth control valve 4-4 is closed; the first compressor 13 is operated, and heat of the refrigerant on the first loop is transferred to the feed liquid in the feed liquid tank 1 through the operation of the first compressor 13;
SC2: the circulating pump 3 operates, and the circulating pump 3 drives the feed liquid to circularly flow in the second loop; the second compressor 14 is operated, and the second compressor 14 compresses the vapor flowing out of the gas-liquid separator 8, flows through the heat exchanger 9, and returns to the water tank 10.
Preferably, a temperature sensor 19 for measuring the temperature of the feed liquid is arranged in the feed liquid tank 1, the first compressor 13 and the second compressor 14 are variable frequency compressors, and the step S02 further comprises the step S03: the first compressor 13 and the second compressor 14 are controlled to operate at different frequencies, respectively, according to the measured value of the temperature sensor.
The principles and processes of the present invention are described below with reference to fig. 1:
The membrane distillation system with the waste heat recovery coupling MVR comprises a material liquid tank 1, a condenser 2, a circulating pump 3, first to seventh control valves 4-1,4-2,4-3,4-4,4-5,4-6,4-7, a membrane component 5, a hollow fiber membrane tube 6, a membrane cavity 7, a gas-liquid separator 8, a heat exchanger 9, a water tank 10, an evaporator 11, a throttling device 12, a first compressor 13, a second compressor 14, a vacuum tank 15, a vacuum pump 16, a fan 17, a liquid level sensor 18 and a temperature sensor 19.
Preferably, the membrane module 5 has a shell-and-tube structure, and includes a plurality of hollow fiber membrane tubes 6 inside which membrane chambers 7 are formed.
Wherein the condenser 2 and the temperature sensor 19 are arranged in the material liquid tank 1; wherein preferably the temperature sensor 19 is located at the bottom of the feed liquid tank 1 and the condenser 2 is located in the middle of the feed liquid tank 1. The feed liquid outlet of the feed liquid tank 1 is connected with the inlet of the circulating pump 3 through a first control valve 4-1, the outlet of the circulating pump 3 is connected with the feed liquid inlet at the upper left side of the membrane assembly 5, the steam outlet at the bottom of the membrane assembly 5 is connected with the inlet of the gas-liquid separator 8, the outlet of the gas-liquid separator 8 is connected with the inlet of the second compressor 14, the outlet of the second compressor 14 is connected with the first inlet of the heat exchanger 9 through a fifth control valve 4-5, and the first outlet of the heat exchanger 9 is connected with the first inlet at the top of the water tank 10 through a third control valve 4-3; the feed liquid outlet at the upper right side of the membrane component 5 is connected with the feed liquid inlet of the heat exchanger 9, namely the cold side inlet, and the feed liquid outlet of the heat exchanger 9, namely the cold side outlet, is connected with the feed liquid inlet at the top of the feed liquid tank 1 through the second control valve 4-2; the vacuum pump 16 is connected with the left lower outlet of the vacuum charging bucket 15, and the top inlet of the vacuum charging bucket 15 is connected with the steam outlet of the gas-liquid separator 8 through the fourth control valve 4-4; the top air outlet of the water tank 10 is connected with a seventh control valve 4-7, and the left upper air inlet is connected with a fan 17 through a sixth control valve 4-6.
The evaporator 11 and the liquid level sensor 18 are arranged in the water tank 10, the liquid level sensor 18 can be positioned in the middle of the water tank 10, the evaporator 11 is positioned at the lower part of the water tank 10, the outlet of the evaporator 11 is connected with the inlet of the first compressor 13, the outlet of the first compressor 13 is connected with the inlet of the condenser 2, the outlet of the condenser 2 is connected with the inlet of the throttling device 12, and the outlet of the throttling device 12 is connected with the inlet of the evaporator 11.
The invention has the following specific working processes: the liquid level sensor 18 detects whether the water tank has preset water amount, when the water amount is insufficient, the first control valve is closed to the fifth control valve 4-1,4-2,4-3,4-4,4-5, the sixth control valve 4-6 and the seventh control valve 4-7 are opened, the first compressor 13 is started, the low-pressure liquid refrigerant throttled by the throttling device 12 absorbs heat in the air to become low-pressure gaseous refrigerant in the evaporator 11, then the low-pressure liquid refrigerant is compressed into high-temperature high-pressure gaseous refrigerant through the first compressor 13 and releases heat to the feed liquid in the condenser 2, the high-pressure low-temperature refrigerant is condensed into high-pressure low-temperature refrigerant by itself to flow to the throttling device 12, the refrigerant circulation is completed, and the waste heat recovery system is an air source heat pump to complete the heating of the feed liquid.
After the liquid in the liquid tank 1 absorbs the heat of the refrigerant and is heated to a preset temperature; the fourth control valve 4-4 is opened, the vacuum pump 16 starts to operate, and the membrane chamber 7 in the hollow fiber membrane tube 6 is in a negative pressure state, i.e., after reaching a predetermined pressure, the fourth control valve 4-4 is closed. The first, second, third and fifth control valves 4-1,4-2,4-3,4-5 are opened, the circulating pump 3 starts to operate, the material liquid is pumped into the shell of the membrane component 5 through the first control valve 4-1 and the circulating pump 3, and partial water and steam of the material liquid close to the wall surface of the membrane enter the membrane cavity 7 through the membrane due to the driving of the pressure difference between the two sides of the membrane of the fiber membrane tube 6; then, pure water vapor separated by the gas-liquid separator 8 enters the second compressor 14 to be heated and pressurized, heat is released to concentrate from the left upper part of the membrane module 5 and from the feed liquid outlet of the membrane module 5 in the heat exchanger 9, the water vapor is condensed into condensed water which is collected in the water tank 10 by the third control valve 4-3, and the heated concentrate flows into the feed liquid tank 1 by the second control valve 4-2 to be concentrated next time.
When the liquid level sensor 18 in the water tank 10 does not sense the water level, the temperature of the liquid in the liquid tank 1 can be adjusted by adjusting the frequency of the second compressor.
When the level sensor 18 in the tank senses the water level, i.e. the water in the tank has a certain amount, the amount may be such that the water level in the tank 10 may be higher than the highest point of the evaporator 11 in the tank 10, or higher than 1/2 of the vertical height of the evaporator 11, etc., or other suitable values as desired by a person skilled in the art. The sixth control valve 4-6,4-7 is closed, the first control valve 4-1, the second control valve 4-2, the third control valve 4-3, the fifth control valve 4-5 is opened, and the fourth control valve 4-4 is closed; the first compressor 13 is operated, and heat of the refrigerant on the first loop is transferred to the feed liquid in the feed liquid tank 1 through the operation of the first compressor 13; the circulating pump 3 operates, and the circulating pump 3 drives the feed liquid to circularly flow in the second loop; the second compressor 14 is operated, and the second compressor 14 compresses the vapor flowing out of the gas-liquid separator 8, flows through the heat exchanger 9, and returns to the water tank.
When the liquid level sensor 18 in the water tank senses the water level, the operation frequency of the first compressor 13 can be adjusted to be high, the frequency of the second compressor 14 is reduced to maintain the constant temperature of the liquid in the liquid tank 1, and at the moment, the waste heat recovery system is formed as a water source heat pump, so that the sensible heat recovery of condensed water is completed.
Preferably, the membrane component 5 is a shell-and-tube type, the shell-and-tube type interior comprises a plurality of hollow fiber membrane tubes 6 which are connected in parallel, the feed liquid enters the shell-and-tube type shell from the lower part of the shell and finally flows out from the upper part of the shell, and water and steam flow out from a membrane cavity 7 in the fiber membrane tubes 6 after being separated out by the membrane.
Preferably, the hollow fiber membrane tube 6 is a hydrophobic membrane, and is made of polytetrafluoroethylene hollow fiber membrane, and the pore diameter is 0.01-0.5 μm.
Preferably, the hollow fiber membrane tube 6 is made of a corrosion resistant material, and the system of the invention can be applied to the evaporation concentration of a highly corrosive solution or a non-highly corrosive solution.
Preferably, the first compressor 13 and the second compressor 14 are variable frequency compressors, and the first compressor 13 and the second compressor 14 are controlled to operate at different frequencies according to data transmitted by the temperature sensor 19.
Preferably, the membrane module 5 is prepared for two sets of equipment to be used alternately in the working process, and the membrane module can be cleaned regularly, so that the service life of the membrane module can be prolonged, and the separation efficiency can be improved.
Preferably, the predetermined pressure of the present invention may be a predetermined vacuum, the predetermined pressure or vacuum acting to precipitate the feed liquid from the membrane.
Preferably, the throttling device 12 of the present invention may be a throttle valve and the second compressor may be a Roots compressor.
Advantageous effects
The membrane distillation system and the method with the waste heat recovery coupling MVR can achieve the following effects: 1) In the feed liquid preheating stage, an air source heat pump is used for replacing electric heating to preheat the feed liquid, so that the energy consumption of the system is reduced; 2) The first compressor 13 and the second compressor 14 are in real-time connection through the liquid level sensor 18 in the water tank 10 and the temperature sensor 19 in the feed liquid tank 1, when the liquid level sensor 18 in the feed liquid tank 1 does not sense the liquid level, the temperature of the feed liquid in the feed liquid tank 1 is kept constant by improving the frequency 14 of the second compressor instead of electric heating, so that the energy consumption of the system is reduced, the operation complexity is further reduced, the running stability of the system is improved, and the labor cost is saved; when the liquid level sensor 18 in the liquid tank 1 senses the liquid level, the liquid temperature of the liquid tank is kept constant by replacing electric heating with a water source heat pump, and the liquid temperature can be kept constant by adjusting the frequency of the first and second compressors 13 and 14, so that the sensible heat of condensate is recovered by the water source heat pump, and the energy consumption of the system is greatly reduced. 3) In the actual working process, the membrane component 5 can be prepared into two sets of same equipment for alternate use and is cleaned at regular time, so that the service life of the membrane component 5 can be prolonged, and the separation efficiency can be improved. 4) Taking an air source heat pump with a heating coefficient cop=q/w=3 as an example to replace electric heating, the same heat is provided for the solution in the feed liquid preheating stage, and the electric heating energy consumption W is 3 times of the energy consumption of the air source heat pump.
Exemplary embodiments of the present disclosure are specifically illustrated and described above. It is to be understood that this disclosure is not limited to the particular arrangements, instrumentalities and methods of implementation described herein; on the contrary, the disclosure is intended to cover various modifications and equivalent arrangements included within the spirit and scope of the appended claims.
Claims (11)
1. The utility model provides a take waste heat recovery coupling MVR's membrane distillation system, includes feed liquid jar (1), condenser (2), water tank (10), evaporimeter (11), first compressor (13), throttling arrangement (12), membrane module (5), circulating pump (3), heat exchanger (9), second compressor (14), vacuum pump (16), its characterized in that:
An evaporator (11) is arranged in the water tank (10), and a condenser (2) is arranged in the feed liquid tank (1), wherein the evaporator (11), the first compressor (13), the condenser (2) and the throttling device (12) form a first loop; the method comprises the following steps: the outlet of the evaporator (11) is communicated with the inlet of the first compressor (13), the outlet of the first compressor (13) is communicated with the inlet of the condenser (2), the outlet of the condenser (2) is communicated with the inlet of the throttling device (12), and the outlet of the throttling device (12) is communicated with the inlet of the evaporator (11);
The material liquid tank (1), the membrane component (5) and the heat exchanger (9) form a second loop; the method comprises the following steps: the feed liquid outlet of the feed liquid tank (1) is communicated with the feed liquid inlet of the membrane component (5), the feed liquid outlet of the membrane component (5) is communicated with the feed liquid inlet of the heat exchanger (9), and the feed liquid outlet of the heat exchanger (9) is communicated with the feed liquid inlet of the feed liquid tank (1); the second loop is also provided with a circulating pump (3), and the circulating pump (3) is used for providing power for the second loop;
The steam outlet of the membrane component (5) is communicated with the inlet of the second compressor (14), the outlet of the second compressor (14) is communicated with the first inlet of the heat exchanger (9), and the first outlet of the heat exchanger (9) is communicated with the first inlet of the water tank (10);
the vacuum pump (16) is communicated with a steam outlet of the membrane component (5);
A liquid level sensor (18) is arranged in the water tank (10), and the liquid level sensor (18) is positioned at a preset height from the bottom of the water tank (10); according to the detection result of the liquid level sensor (18), the membrane distillation system operates according to a first or second operation mode;
At least one of the first compressor (13) and the second compressor (14) is a variable frequency compressor; the water tank (10) further comprises an air inlet and an air outlet;
a temperature sensor (19) for measuring the temperature of the feed liquid is arranged in the feed liquid tank (1);
The liquid level sensor (18) is positioned at a preset height from the bottom of the water tank (10), a temperature sensor (19) for measuring the temperature of the liquid is arranged in the liquid tank (1), and the first compressor (13) and the second compressor (14) are variable-frequency compressors;
The control method of the membrane distillation system comprises the following steps: s01: acquiring a detection result of a liquid level sensor (18); s02: when the liquid level is not detected, controlling the membrane distillation system to operate according to a first operation mode; when the liquid level is detected, controlling the membrane distillation system to operate according to a second operation mode; step S03 is further included after step S02: controlling the first compressor (13) and the second compressor (14) to operate at different frequencies respectively according to the measured value of the temperature sensor;
a first control valve (4-1) is formed between a second loop feeding liquid tank (1) and a membrane component (5) of the membrane distillation system, and a second control valve (4-2) is formed between a second loop upper heat exchanger (9) and a feed liquid tank (1); a third control valve (4-3) is arranged between the first outlet of the heat exchanger (9) and the first inlet of the water tank (10); the steam outlet of the membrane component (5) is communicated with the inlet of the second compressor (14) through the gas-liquid separator (8), the vacuum pump (16) is communicated with the outlet of the vacuum material tank (15), and the inlet of the vacuum material tank (15) is communicated with the inlet or the outlet of the gas-liquid separator (8) through the fourth control valve (4-4); a fifth control valve (4-5) is arranged between the outlet of the second compressor (14) and the first inlet of the heat exchanger (9); a sixth control valve (4-6) is arranged at the air inlet of the water tank (10), and a seventh control valve (4-7) is arranged at the air outlet of the water tank (10);
The first operation mode comprises the following steps: SA1, a sixth control valve and a seventh control valve (4-6, 4-7) are opened, the first control valve to the fifth control valve (4-1, 4-2,4-3,4-4, 4-5) are closed, the first compressor (13) starts to operate, and the heat of the refrigerant on the first loop is transferred to the feed liquid of the feed liquid tank (1) through the operation of the first compressor (13);
SA2, acquiring the temperature of the feed liquid detected by a temperature sensor (19);
SA3, when the temperature of the feed liquid reaches a first preset temperature, a fourth control valve (4-4) is opened, a vacuum pump (16) starts to operate, and when the steam outlet of the membrane assembly (5) reaches a preset pressure, the fourth control valve (4-4) is closed; opening a first control valve (4-1, a second control valve, a third control valve and a fifth control valve (4-1, 4-2,4-3, 4-5), starting the circulation pump (3), and enabling the circulation pump (3) to drive the feed liquid to circularly flow in a second loop; the second compressor (14) starts to operate, and the second compressor (14) compresses the steam flowing out of the gas-liquid separator (8), flows through the heat exchanger (9) and returns to the water tank (10);
the second mode of operation includes the steps of: SC1: the sixth control valve (4-6, 4-7) is closed, the first control valve (4-1, 4-2,4-3, 4-5) is opened, the second control valve (4-4) is closed; the first compressor (13) operates, and heat of the refrigerant on the first loop is transferred to feed liquid in the feed liquid tank (1) through the operation of the first compressor (13);
SC2: the circulating pump (3) operates, and the circulating pump (3) drives the feed liquid to circularly flow in the second loop; the second compressor (14) is operated, and the second compressor (14) compresses the vapor flowing out of the gas-liquid separator (8), flows through the heat exchanger (9), and returns to the water tank (10).
2. The membrane distillation system according to claim 1, wherein: the steam outlet of the membrane component (5) is communicated with the inlet of the second compressor (14) after passing through the gas-liquid separator (8).
3. The membrane distillation system according to claim 2, wherein: the device also comprises a vacuum material tank (15), wherein a vacuum pump (16) is communicated with an outlet of the vacuum material tank (15), and an inlet of the vacuum material tank (15) is communicated with an inlet or an outlet of the gas-liquid separator (8) through a fourth control valve (4-4).
4. A membrane distillation system according to claim 3, wherein: the air conditioner further comprises a fan (17), and the fan (17) is used for accelerating circulation of air in the water tank (10).
5. The membrane distillation system according to any of claims 1-4, wherein: a first control valve (4-1) is formed between the second loop feeding liquid tank (1) and the membrane component (5), and a second control valve (4-2) is formed between the second loop upper heat exchanger (9) and the feed liquid tank (1).
6. The membrane distillation system according to any of claims 1-4, wherein: a third control valve (4-3) is arranged between the first outlet of the heat exchanger (9) and the first inlet of the water tank (10).
7. The membrane distillation system according to any of claims 1-4, wherein: a fifth control valve (4-5) is arranged between the outlet of the second compressor (14) and the first inlet of the heat exchanger (9).
8. A method of controlling a membrane distillation system according to any of claims 1 to 7, wherein: the water tank (10) of the membrane distillation system is internally provided with a liquid level sensor (18), the liquid level sensor (18) is positioned at a preset height from the bottom of the water tank (10), and the control method comprises the following steps: s01: acquiring a detection result of a liquid level sensor (18); s02: when the liquid level is not detected, controlling the membrane distillation system to operate according to a first operation mode; when the liquid level is detected, the membrane distillation system is controlled to operate in a second mode of operation.
9. The control method according to claim 8, characterized in that; a first control valve (4-1) is formed between a second loop feeding liquid tank (1) and a membrane component (5) of the membrane distillation system, and a second control valve (4-2) is formed between a second loop upper heat exchanger (9) and a feed liquid tank (1); a third control valve (4-3) is arranged between the first outlet of the heat exchanger (9) and the first inlet of the water tank (10); the steam outlet of the membrane component (5) is communicated with the inlet of the second compressor (14) through the gas-liquid separator (8), the vacuum pump (16) is communicated with the outlet of the vacuum material tank (15), and the inlet of the vacuum material tank (15) is communicated with the inlet or the outlet of the gas-liquid separator (8) through the fourth control valve (4-4); a fifth control valve (4-5) is arranged between the outlet of the second compressor (14) and the first inlet of the heat exchanger (9); a sixth control valve (4-6) is arranged at the air inlet of the water tank (10), and a seventh control valve (4-7) is arranged at the air outlet of the water tank (10); a temperature sensor (19) for measuring the temperature of the feed liquid is arranged in the feed liquid tank (1);
The first operation mode comprises the following steps: SA1, a sixth control valve and a seventh control valve (4-6, 4-7) are opened, the first control valve to the fifth control valve (4-1, 4-2,4-3,4-4, 4-5) are closed, the first compressor (13) starts to operate, and the heat of the refrigerant on the first loop is transferred to the feed liquid of the feed liquid tank (1) through the operation of the first compressor (13);
SA2, acquiring the temperature of the feed liquid detected by a temperature sensor (19);
SA3, when the temperature of the feed liquid reaches a first preset temperature, a fourth control valve (4-4) is opened, a vacuum pump (16) starts to operate, and when the steam outlet of the membrane assembly (5) reaches a preset pressure, the fourth control valve (4-4) is closed; opening a first control valve (4-1, a second control valve, a third control valve and a fifth control valve (4-1, 4-2,4-3, 4-5), starting the circulation pump (3), and enabling the circulation pump (3) to drive the feed liquid to circularly flow in a second loop; the second compressor (14) starts to operate, and the second compressor (14) compresses the steam flowing out of the gas-liquid separator (8), flows through the heat exchanger (9), and returns to the water tank (10).
10. The control method according to any one of claims 8 to 9, characterized in that; a first control valve (4-1) is formed between a second loop feeding liquid tank (1) and a membrane component (5) of the membrane distillation system, and a second control valve (4-2) is formed between a second loop upper heat exchanger (9) and a feed liquid tank (1); a third control valve (4-3) is arranged between the first outlet of the heat exchanger (9) and the first inlet of the water tank (10); the steam outlet of the membrane component (5) is communicated with the inlet of the second compressor (14) through the gas-liquid separator (8), the vacuum pump (16) is communicated with the outlet of the vacuum material tank (15), and the inlet of the vacuum material tank (15) is communicated with the inlet or the outlet of the gas-liquid separator (8) through the fourth control valve (4-4); a fifth control valve (4-5) is arranged between the outlet of the second compressor (14) and the first inlet of the heat exchanger (9); a sixth control valve (4-6) is arranged at the air inlet of the water tank (10), and a seventh control valve (4-7) is arranged at the air outlet of the water tank (10);
the second mode of operation includes the steps of: SC1: the sixth control valve (4-6, 4-7) is closed, the first control valve (4-1, 4-2,4-3, 4-5) is opened, the second control valve (4-4) is closed; the first compressor (13) operates, and heat of the refrigerant on the first loop is transferred to feed liquid in the feed liquid tank (1) through the operation of the first compressor (13);
SC2: the circulating pump (3) operates, and the circulating pump (3) drives the feed liquid to circularly flow in the second loop; the second compressor (14) is operated, and the second compressor (14) compresses the vapor flowing out of the gas-liquid separator (8), flows through the heat exchanger (9), and returns to the water tank (10).
11. The control method according to any one of claims 8 to 9, characterized in that; be equipped with in feed liquid jar (1) and be used for measuring temperature sensor (19) of feed liquid temperature, first compressor (13) and second compressor (14) are the variable frequency compressor, still include step S03 after step S02: the first compressor (13) and the second compressor (14) are controlled to operate at different frequencies, respectively, based on the measured values of the temperature sensor.
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| CN111473660B (en) * | 2020-04-10 | 2021-09-17 | 东南大学 | Heat source tower solution regeneration system based on vacuum membrane distillation |
| CN115028235A (en) * | 2022-05-30 | 2022-09-09 | 江苏格林环创科技有限公司 | Low temperature heat pump membrane distillation waste water concentration system |
| TWI834218B (en) * | 2022-07-13 | 2024-03-01 | 睿鍀水資源科技股份有限公司 | liquid handling system |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH067644A (en) * | 1992-06-25 | 1994-01-18 | Hitachi Ltd | Film distillation apparatus |
| JP2002016036A (en) * | 2000-06-27 | 2002-01-18 | Shin Etsu Handotai Co Ltd | Method of wastewater reclamation and exhaust heat recovery |
| CN2475724Y (en) * | 2000-12-22 | 2002-02-06 | 清华大学 | Water treatment device by pressure reducing film distillation |
| CN104190260A (en) * | 2014-09-19 | 2014-12-10 | 天津工业大学 | Decompression combination airgap membrane distillation method and device thereof |
| CN205061622U (en) * | 2015-08-13 | 2016-03-02 | 大唐环境产业集团股份有限公司 | Efficient membrane distillation plant |
| CN206199023U (en) * | 2016-11-23 | 2017-05-31 | 厦门鲲扬膜科技有限公司 | A kind of distillation device of carrying vapour mechanical compress |
| CN107651727A (en) * | 2017-10-19 | 2018-02-02 | 南京航空航天大学 | Double-effect heat pump film steam sewage disposal system and method |
| CN108622983A (en) * | 2017-03-15 | 2018-10-09 | 中国石油化工股份有限公司 | A kind of novel distillation device of coupling heat recovery system |
| CN108619915A (en) * | 2017-03-15 | 2018-10-09 | 中国石油化工股份有限公司 | A kind of gas source type heat pump solar energy membrane distillation hybrid system |
| CN110404411A (en) * | 2019-07-22 | 2019-11-05 | 珠海格力电器股份有限公司 | A kind of membrane distillation system and method recycling coupling MVR with waste heat |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103900251B (en) * | 2012-12-25 | 2016-03-30 | 福州斯狄渢电热水器有限公司 | Immediately heating water heater |
-
2019
- 2019-07-22 CN CN201910658991.5A patent/CN110404411B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH067644A (en) * | 1992-06-25 | 1994-01-18 | Hitachi Ltd | Film distillation apparatus |
| JP2002016036A (en) * | 2000-06-27 | 2002-01-18 | Shin Etsu Handotai Co Ltd | Method of wastewater reclamation and exhaust heat recovery |
| CN2475724Y (en) * | 2000-12-22 | 2002-02-06 | 清华大学 | Water treatment device by pressure reducing film distillation |
| CN104190260A (en) * | 2014-09-19 | 2014-12-10 | 天津工业大学 | Decompression combination airgap membrane distillation method and device thereof |
| CN205061622U (en) * | 2015-08-13 | 2016-03-02 | 大唐环境产业集团股份有限公司 | Efficient membrane distillation plant |
| CN206199023U (en) * | 2016-11-23 | 2017-05-31 | 厦门鲲扬膜科技有限公司 | A kind of distillation device of carrying vapour mechanical compress |
| CN108622983A (en) * | 2017-03-15 | 2018-10-09 | 中国石油化工股份有限公司 | A kind of novel distillation device of coupling heat recovery system |
| CN108619915A (en) * | 2017-03-15 | 2018-10-09 | 中国石油化工股份有限公司 | A kind of gas source type heat pump solar energy membrane distillation hybrid system |
| CN107651727A (en) * | 2017-10-19 | 2018-02-02 | 南京航空航天大学 | Double-effect heat pump film steam sewage disposal system and method |
| CN110404411A (en) * | 2019-07-22 | 2019-11-05 | 珠海格力电器股份有限公司 | A kind of membrane distillation system and method recycling coupling MVR with waste heat |
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