CN115962586B - Direct solar adsorption brine concentration refrigeration system and use method - Google Patents
Direct solar adsorption brine concentration refrigeration system and use method Download PDFInfo
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- CN115962586B CN115962586B CN202211642071.2A CN202211642071A CN115962586B CN 115962586 B CN115962586 B CN 115962586B CN 202211642071 A CN202211642071 A CN 202211642071A CN 115962586 B CN115962586 B CN 115962586B
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- 239000012267 brine Substances 0.000 title claims abstract description 80
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 79
- 238000000034 method Methods 0.000 title claims abstract description 37
- 238000001179 sorption measurement Methods 0.000 title claims abstract description 36
- 238000005057 refrigeration Methods 0.000 title claims abstract description 23
- 239000003463 adsorbent Substances 0.000 claims abstract description 82
- 239000006096 absorbing agent Substances 0.000 claims abstract description 27
- 239000000463 material Substances 0.000 claims description 78
- 239000006260 foam Substances 0.000 claims description 68
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 51
- 229910052751 metal Inorganic materials 0.000 claims description 45
- 239000002184 metal Substances 0.000 claims description 45
- 239000011248 coating agent Substances 0.000 claims description 40
- 238000000576 coating method Methods 0.000 claims description 40
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 38
- 239000000741 silica gel Substances 0.000 claims description 38
- 229910002027 silica gel Inorganic materials 0.000 claims description 38
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 37
- 229910052802 copper Inorganic materials 0.000 claims description 37
- 239000010949 copper Substances 0.000 claims description 37
- 239000002131 composite material Substances 0.000 claims description 27
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 12
- 239000013178 MIL-101(Cr) Substances 0.000 claims description 8
- 239000006229 carbon black Substances 0.000 claims description 8
- 238000003795 desorption Methods 0.000 claims description 8
- 229910021389 graphene Inorganic materials 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- 238000005286 illumination Methods 0.000 claims description 5
- 238000004891 communication Methods 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 claims description 2
- 239000002826 coolant Substances 0.000 claims description 2
- 239000003651 drinking water Substances 0.000 abstract description 15
- 235000020188 drinking water Nutrition 0.000 abstract description 15
- 150000002500 ions Chemical class 0.000 abstract description 8
- 238000004064 recycling Methods 0.000 abstract description 3
- 239000013505 freshwater Substances 0.000 description 31
- 238000001704 evaporation Methods 0.000 description 23
- 230000008020 evaporation Effects 0.000 description 22
- 239000013535 sea water Substances 0.000 description 18
- 239000007788 liquid Substances 0.000 description 15
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 10
- 150000003839 salts Chemical class 0.000 description 10
- 239000000498 cooling water Substances 0.000 description 9
- 238000010612 desalination reaction Methods 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 239000013177 MIL-101 Substances 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 6
- 229910052782 aluminium Inorganic materials 0.000 description 5
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 5
- 239000002041 carbon nanotube Substances 0.000 description 5
- 229910021393 carbon nanotube Inorganic materials 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 229910052759 nickel Inorganic materials 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 3
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 3
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 3
- 238000000909 electrodialysis Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 229910052500 inorganic mineral Inorganic materials 0.000 description 3
- 229910052744 lithium Inorganic materials 0.000 description 3
- 239000011777 magnesium Substances 0.000 description 3
- 229910052749 magnesium Inorganic materials 0.000 description 3
- 239000011707 mineral Substances 0.000 description 3
- 239000011591 potassium Substances 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000035622 drinking Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000002336 sorption--desorption measurement Methods 0.000 description 2
- 241000554155 Andes Species 0.000 description 1
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 239000011358 absorbing material Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 235000020682 bottled natural mineral water Nutrition 0.000 description 1
- -1 brine ion Chemical class 0.000 description 1
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 1
- 229910052794 bromium Inorganic materials 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 229910000365 copper sulfate Inorganic materials 0.000 description 1
- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002384 drinking water standard Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000005338 heat storage Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000003014 ion exchange membrane Substances 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000006262 metallic foam Substances 0.000 description 1
- 239000002366 mineral element Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229910001414 potassium ion Inorganic materials 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
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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
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
Landscapes
- Sorption Type Refrigeration Machines (AREA)
Abstract
The utility model provides a direct solar adsorption brine concentration refrigeration system and a use method thereof, and belongs to the technical field of resource utilization. The utility model comprises the following steps: an evaporator; a condenser; one end of the first adsorber is communicated with the evaporator, and the other end of the first adsorber is communicated with the condenser; one end of the second adsorber is communicated with the evaporator, and the other end of the second adsorber is communicated with the condenser; the first absorber and the second absorber are integrated with a solar heat collector, and an adsorbent with direct photo-thermal property is arranged in the first absorber and the second absorber; the evaporator, the condenser, the first adsorber and the second adsorber are all provided with valves on the pipelines communicated with each other, and the condenser is also provided with valves. According to the utility model, the solar heat collector is integrated on the absorber, the adsorbent with direct photo-thermal property is arranged in the absorber, the evaporated brine is continuously absorbed and desorbed, the brine is directly concentrated by using solar energy, and the refrigeration and direct drinking water can be realized while the recycling of ions in the concentrated brine is realized.
Description
Technical Field
The utility model relates to the technical field of resource utilization, in particular to a direct solar adsorption brine concentration refrigeration system, a use method and co-production direct drinking water.
Background
The world seawater and salt lake brine resources are quite rich, and the seawater area accounts for about 71% of the total surface area. Salt lake brine is a water resource with high concentration of mineral salts, and lithium-rich salt lakes are widely distributed throughout the world, mainly in the south american andes plateau of south america, the Qinghai-Tibet plateau of China, and the northwest region of north america. The seawater (brine) contains rich sodium, potassium, magnesium, lithium, chlorine, bromine and other resources, and the existing seawater (brine) resource utilization mode mainly comprises seawater (brine) desalination, seawater (brine) concentration salt preparation, seawater (brine) lithium extraction, seawater (brine) magnesium extraction and the like.
The sea water desalination methods for realizing installed application in the world at present mainly fall into two main categories: firstly, a heat treatment process mainly comprises multi-stage flash evaporation (MSF) and multi-effect evaporation (MED); second is a membrane treatment process such as Electrodialysis (ED) and reverse osmosis (SWRO). Practical application shows that: the prior art still has obvious defects such as consumption of high-grade energy sources and emission of pollutants at the expense of electric energy or a large amount of fuel, corrosion and blockage of a membrane/mass exchanger, high maintenance cost caused by pipeline corrosion or salt accumulation or scale deposition on the outer surface of the heat exchanger, and along with the increasing shortage of the energy sources, the fresh water prepared by the two methods has high cost
The existing brine concentration salt-making technology mainly comprises a salt-burning method, a vacuum salt-making method, an electrodialysis method and the like. The solar salt-burning method has low solar energy utilization rate and low production efficiency, is extremely easy to be influenced by weather, occupies large area of salt field and has a certain degree of harm to soil. The utility model with publication number of CN212315564U discloses a device for accelerating the salt burning of seawater, which utilizes a vertical plate array of light absorbing materials to improve the absorptivity of the seawater to solar energy and simultaneously fully contacts natural wind to accelerate the evaporation of water; the utility model with publication number of CN205709901U discloses a sea water salt-burning and desalination integrated system, which is not affected by weather, salt can be produced all the year round, and evaporated water can be collected to obtain fresh water by adding a condensing system, but the system is still affected by sun illumination and cannot work at night. The modern vacuum salt making technology can separate water quickly through a multi-stage flash evaporation technology, has higher salt making efficiency, but has more complex technology and higher energy consumption. The electrodialysis method uses ion exchange membrane to separate and concentrate salt water under the action of potential difference pushing force, and has high salt-making efficiency and high energy consumption. The utility model with publication number of CN213679909U discloses an adsorption type sea water desalination system, which promotes brine evaporation to realize refrigeration through the adsorption effect of an adsorbent, and the water vapor desorbed by the adsorbent is condensed and released in a condenser to obtain fresh water, thereby having the functions of sea water desalination and cold/heat accumulation. The utility model with publication number of CN202430029U discloses a solar adsorption type sea water desalting device with a heat recovery and mass recovery circulation, and hot water obtained by a solar heat collector drives an adsorbent desorption process. However, the existing adsorption type sea water desalination technology needs to indirectly utilize solar energy through a solar heat collector, so that the solar energy cannot be directly and efficiently utilized, and meanwhile, the technology omits the recycling utilization of concentrated brine.
Disclosure of Invention
In view of this, in order to solve the technical problems that the existing adsorption type sea water desalination technology needs to indirectly utilize solar energy through a solar heat collector and cannot directly and efficiently utilize the solar energy, on one hand, the utility model provides a direct solar adsorption brine concentration refrigeration system.
In order to solve the technical problems, the utility model provides the following technical scheme:
a direct solar adsorption brine concentration refrigeration system comprising:
an evaporator;
a condenser;
a first adsorber having one end connected to the evaporator and the other end connected to the condenser;
a second adsorber, one end of which is communicated with the evaporator, and the other end of which is communicated with the condenser;
the first absorber and the second absorber are integrated with a solar heat collector, and an adsorbent with direct photo-thermal performance is arranged in the first absorber and the second absorber;
the evaporator, the condenser, the first adsorber and the second adsorber are all provided with valves on the pipelines communicated with each other, and the condenser is also provided with a valve.
Preferably, the device further comprises an auxiliary device;
the auxiliary device is used for cooling or heating the first adsorber and the second adsorber.
Preferably, the auxiliary device has a cold/hot water inlet and a cold/hot water outlet, which are in communication with the heat exchange tubes in the first adsorber and the second adsorber, respectively, via a pipeline.
Preferably, the adsorbent is a foam metal solidified composite adsorbent with a photo-thermal material coated on the surface, and the foam metal solidified composite adsorbent consists of a water absorbing adsorbent, foam metal and a photo-thermal material coating material.
Preferably, the photo-thermal material coating material is 0.5-5% by mass, the foam metal is 31-62% by mass, and the water absorbing adsorbent is 37-64% by mass.
Preferably, the adsorbent is a foam metal solidified MIL-101 composite adsorbent with a photo-thermal material coating on the surface, wherein the mass percentage of MIL-101 is 37%, the mass percentage of foam metal is 62%, and the mass percentage of photo-thermal material is 1%;
wherein, the photo-thermal material is preferably graphene oxide, and the foam metal is copper foam.
Preferably, the adsorbent is a foam metal cured silica gel composite adsorbent with a photo-thermal material coating on the surface, wherein the mass percentage of silica gel is 44% -64%, the mass percentage of photo-thermal material is 1% -5%, and the mass percentage of foam metal is 31% -47%;
preferably, the mass percentage of the silica gel is 55%, the mass percentage of the foam metal is foam copper, the mass percentage of the foam copper is 44%, the photo-thermal material is carbon black, and the mass percentage of the carbon black is 1%.
Preferably, the adsorbent is a foam metal SAPO-34 composite adsorbent or CuSO with the surface coated with a photo-thermal material coating 4 When the adsorbent is a foamed metal solidified SAPO-34 composite adsorbent with a photo-thermal material coating on the surface, the mass percentage of the SAPO-34 is 58% -58.5%, the mass percentage of the foamed metal is 41%, and the mass percentage of the photo-thermal material is 0.5% -1%;
when the adsorbent is foamed metal solidified CuSO with the surface coated with photo-thermal material coating 4 When the adsorbent is compounded, cuSO 4 44% by mass, 55% by mass of foam metal and 1% by mass of photo-thermal material.
On the other hand, the utility model also provides a using method of the direct solar adsorption brine concentration refrigeration system, which comprises the following steps:
1) Adding brine into an evaporator, and opening a valve between the evaporator and a first adsorber to perform adsorption;
2) Closing a valve between the evaporator and the first adsorber after the adsorption is completed, opening the valve between the first adsorber and the condenser and the valve on the condenser when the temperature of the first adsorber reaches the desorption temperature, and simultaneously opening the valve between the evaporator and the second adsorber to enable the second adsorber to adsorb;
3) When the second adsorber is completed, closing valves between the evaporator and the first adsorber and between the second adsorber, closing valves on the condenser, opening valves between the first adsorber, the second adsorber and the condenser, enabling the first adsorber to be communicated with the second adsorber for returning the quality, and closing the valves between the first adsorber, the second adsorber and the condenser after the quality returning is completed;
4) And after the first adsorber and the second adsorber reach adsorption and desorption temperatures respectively, opening a valve between the evaporator and the first adsorber, opening a valve between the second adsorber and the condenser and opening a valve on the condenser.
Preferably, when the illumination is insufficient, the auxiliary device introduces a heat medium into the second adsorber as auxiliary energy to heat the pyrolysis water;
the auxiliary device introduces a cooling medium into the first adsorber to cool the first adsorber.
Compared with the prior art, the utility model has the following beneficial effects:
according to the direct solar adsorption brine concentration refrigeration system provided by the utility model, the solar heat collector is integrated on the absorber, the absorber with direct photo-thermal property is arranged in the absorber, the evaporated brine is continuously adsorbed and desorbed, the brine is directly concentrated by using solar energy, and the refrigeration and direct drinking water can be realized while the recycling utilization of ions in the concentrated brine is realized.
The direct solar energy adsorption brine concentration refrigeration system and the application method thereof provided by the utility model can be used for directly heating and desorbing the adsorption brine concentration refrigeration co-production fresh water system by solar energy, and the brine concentration, refrigeration and fresh water generation are carried out by utilizing solar energy, so that the system is four in one; the system has simple structure, is easy to operate, is little affected by weather, and can be operated continuously day and night.
Drawings
FIG. 1 is a schematic diagram of a direct solar adsorption brine concentration refrigeration system of the present utility model;
in the figure, 1 a first adsorber, 2 a second adsorber, 3 an evaporator, 4 an evaporator inlet line, 5 an evaporator outlet line, 6 a heat exchange coil, 7 a condenser, 8 a condensate inlet, 9 a condensate outlet, 10 a direct drinking water outlet line, 11 a cold/hot water inlet, 12 a cold/hot water outlet, 13 a first valve, 14 a second valve, 15 a third valve, 16 a fourth valve, 17 a condenser valve, 18 a direct drinking water storage tank.
Detailed Description
The technical solutions in the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model; it is apparent that the described embodiments are only some embodiments of the present utility model, not all embodiments, and that all other embodiments obtained by persons of ordinary skill in the art without making creative efforts based on the embodiments in the present utility model are within the protection scope of the present utility model.
In the description of the present utility model, it should be noted that the positional or positional relationship indicated by the terms such as "upper", "lower", "inner", "outer", "top/bottom", etc. are based on the positional or positional relationship shown in the drawings, are merely for convenience of describing the present utility model and simplifying the description, and do not indicate or imply that the apparatus or elements referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as limiting the present utility model. Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present utility model, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "configured to," "engaged with," "connected to," and the like are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present utility model will be understood in specific cases by those of ordinary skill in the art.
As shown in fig. 1, the present utility model provides a direct solar adsorption brine concentration refrigeration system, comprising:
an evaporator 3;
a condenser 7;
a first adsorber 1 having one end connected to the evaporator 3 and the other end connected to the condenser 7;
a second adsorber 2 having one end connected to the evaporator 3 and the other end connected to the condenser 7;
the first absorber 1 and the second absorber 2 are integrated with a solar heat collector, and an adsorbent with direct photo-thermal performance is arranged in the solar heat collector;
the evaporator 3, the condenser 7, the first adsorber 1 and the second adsorber 2 are all provided with valves on the pipes connected with each other, and the condenser 7 is also provided with a valve.
In the utility model, the device also comprises an auxiliary device;
the auxiliary device is used for cooling or heating the first adsorber 1 and the second adsorber 2.
In the present utility model, the auxiliary device has a cold/hot water inlet 11 and a cold/hot water outlet 12, which are respectively connected to the heat exchange tubes in the first adsorber 1 and the second adsorber 2 by pipes.
According to the direct solar adsorption brine concentration refrigeration system provided by the utility model, the evaporator 3 is preferably provided with an evaporator inlet pipeline 4 and an evaporator outlet pipeline 5, brine is introduced into the evaporator 3 through the evaporator inlet pipeline 4, and concentrated brine is discharged through the evaporator outlet pipeline 5;
the evaporator 3 is preferably provided with a heat exchange coil 6, and the heat exchange coil 6 can obtain low-temperature cooling water.
The condenser 7 can adopt air cooling or water cooling, the condensation temperature can be 10-35 ℃, the condenser is provided with a condensate water inlet 8 and a condensate water outlet 9, condensate water enters the condenser from the condensate water inlet 8, flows out from the condensate water outlet 9, and water vapor desorbed from the first adsorber 1 and the second adsorber 2 enters the condenser 7 to be condensed to obtain purified fresh water, and flows into the direct drinking water storage tank 18 through the direct drinking water outlet pipeline to be stored.
The valve between the evaporator 3 and the first adsorber 1 is a first valve 13, the valve between the evaporator 3 and the second adsorber 2 is a second valve 14, the valve between the first adsorber 1 and the condenser 7 is a third valve 15, the valve between the second adsorber 2 and the condenser 7 is a fourth valve 16, and the valve on the condenser 7 is a condenser valve 17.
In the utility model, the adsorbent is a foam metal solidified composite adsorbent with a photo-thermal material coated on the surface, and the adsorbent consists of a water absorbing adsorbent, foam metal and a photo-thermal material coating material.
In the utility model, the photo-thermal material coating material accounts for 0.5-5% by mass, the foam metal accounts for 31-62% by mass, and the water absorbing adsorbent accounts for 37-64% by mass.
In the utility model, the adsorbent is a foam metal solidified MIL-101 composite adsorbent with a photo-thermal material coating on the surface, wherein the mass percentage of MIL-101 is 37%, the mass percentage of foam metal is 62%, and the mass percentage of photo-thermal material is 1%;
in the present utility model, the photo-thermal material is preferably graphene oxide, and the metal foam is copper foam.
In the utility model, the adsorbent is a foam metal solidified silica gel composite adsorbent with a photo-thermal material coating on the surface, wherein the mass percent of silica gel is 44% -64%, the mass percent of photo-thermal material is 1% -5%, and the mass percent of foam metal is 31% -47%;
in the utility model, the mass percentage of the silica gel is 55%, the foam metal is foam copper, the mass percentage of the foam copper is 44%, the photo-thermal material is carbon black, and the mass percentage of the carbon black is 1%.
In the utility model, the adsorbent is a foam metal SAPO-34 composite adsorbent or CuSO with the surface coated with a photo-thermal material coating 4 When the adsorbent is a foamed metal solidified SAPO-34 composite adsorbent with a photo-thermal material coating on the surface, the mass percentage of the SAPO-34 is 58% -58.5%, the mass percentage of the foamed metal is 41%, and the mass percentage of the photo-thermal material is 0.5% -1%;
when the adsorbent is foamed metal solidified CuSO with the surface coated with photo-thermal material coating 4 When the adsorbent is compounded, cuSO 4 44% by mass, 55% by mass of foam metal and 1% by mass of photo-thermal material.
The utility model is characterized in that an adsorbent with direct photo-thermal property is arranged in an absorber and is used for adsorbing brine in the evaporator 3, and the adsorbent absorbs water to realize concentration of the brine and drive the brine in the evaporator 3 to evaporate, absorb heat and refrigerate; after the adsorbent is saturated by water absorption, the solar energy directly irradiates the adsorber to realize photo-thermal conversion, the adsorbent is heated to promote desorption of water vapor in the adsorbent, purified direct drinking water meeting national standards can be obtained after condensation by the condenser 7, and continuous brine concentration, solar energy adsorption refrigeration and co-production of direct drinking water can be realized.
In the utility model, heat insulation layers can be arranged outside the first absorber 1, the first absorber 2, the evaporator 3 and various pipelines, the first absorber 1 and the first absorber 2 can be flat plates and round tubes, and the tube walls are vacuum glass; the first adsorber 1 and the first adsorber 2 are internally provided with heat exchange tubes, temperature and pressure sensors.
In the utility model, the brine can be salt lake brine, seawater, geothermal water, saline wastewater and the like, and has no special requirement; the heat medium can be hot water, the cold medium can be cooling water, the temperature of the cooling water for reducing the temperature of the absorber can be 20-35 ℃, the hot water can be heated by any one or two modes of solar energy, geothermal energy, wind energy and the like, the temperature of the hot water is 55-95 ℃, and the evaporation temperature of the evaporator 3 can be 10-50 ℃.
In the utility model, the water absorbing adsorbent is any one or two of silica gel, MIL-101, SAPO-34 and copper sulfate, the foam metal is any one or two of foam copper, foam aluminum and foam nickel, and the photo-thermal material coating material is any one or two of carbon black, graphene oxide, carbon nano tube, perovskite and nano metal;
on the other hand, the utility model also provides a using method of the direct solar adsorption brine concentration refrigeration system, which comprises the following steps:
1) Before the system runs, the whole system and the absorber are vacuumized, and all valves are closed. The brine is added into the evaporator 3, the first valve 13 is opened, the evaporator 3 is communicated with the first adsorber 1, the brine in the evaporator 3 is continuously evaporated and concentrated, heat is taken away by evaporation, and the heat exchange coil 6 can obtain low-temperature cooling water.
2) After adsorption for a certain time, the first valve 13 is closed, the first adsorber 1 is integrated with a solar heat collector, and hot water (a heat storage tank) can be introduced into copper tubes at the bottom of the first adsorber 1 from the cold/hot water inlet 11 to serve as an auxiliary heat source when illumination is insufficient at night, in overcast and rainy days and the like.
3) When the temperature of the first adsorber 1 reaches the desorption temperature, the valve third valve 15 and the condenser valve 17 are opened, and the water vapor desorbed from the first adsorber 1 enters the condenser 7 to be condensed, so that purified fresh water flows into the direct drinking water storage tank 18 through the direct drinking water outlet pipeline 10 to be stored. Simultaneously, the second valve 14 is opened, the evaporator 3 is communicated with the second adsorber 2, and the brine in the evaporator 3 is continuously evaporated and concentrated and takes away heat.
4) When a certain adsorption/desorption time is reached, the first valve 13, the second valve 14 and the condenser valve 17 are closed, the third valve 15 and the fourth valve 16 are opened, the first adsorber 1 and the second adsorber 2 are communicated for returning the mass, and after the mass returning is finished, the third valve 15 and the fourth valve 16 are closed.
5) Cooling water is introduced into copper tubes at the bottom of the first adsorber 1 from the cold/hot water inlet 11 to cool the first adsorber 1, and flows out from the cold/hot water outlet 12. The second adsorber 2 is integrated with a solar collector, and hot water can be introduced into copper tubes at the bottom of the second adsorber 2 from a cold/hot water inlet 11 to serve as an auxiliary heat source when the illumination is insufficient.
6) After the first adsorber 1 and the second adsorber 2 reach the adsorption/desorption temperatures, the flow of cooling water to the first adsorber 1 is stopped. Opening a first valve 13, communicating the evaporator 3 with the first adsorber 1, and continuously evaporating and concentrating brine in the evaporator 4 to take heat away; simultaneously, the fourth valve 16 is opened, the water vapor desorbed from the second adsorber 2 enters the condenser 7 to be condensed to obtain purified fresh water, and the purified fresh water flows into the direct drinking water storage tank 18 through the direct drinking water outlet pipeline 10 to be stored.
The continuous solar adsorption brine concentration and fresh water co-production of the double beds can be realized by repeating the steps 3-6.
After the brine reaches the required concentration, the first valve 13 and the second valve 14 are closed, and the concentrated brine is discharged from the evaporator outlet pipeline 5. And (3) adding fresh brine subjected to degassing pretreatment into the evaporator 4 again, repeating the steps 3-6 again after performing the steps 1-2, and realizing double-bed continuous solar adsorption brine concentration and fresh water cogeneration again.
The technical scheme of the present utility model is clearly explained in detail below in conjunction with specific examples.
GO in the following examples is abbreviated as graphene oxide, wherein MIL-101 is preferably MIL-101 (Cr), SAPO-34 can be selected from conventional products on the market, and GrO is reduced graphene oxide.
Example 1
The adsorbent is a foam copper solidified silica gel composite adsorbent coated with a 1% GO photo-thermal material coating, the mass percentage of silica gel is 55%, the mass percentage of foam copper is 44%, the solid-liquid ratio of silica gel to brine is 2.2, and the circulation time is 5 hours. And vacuumizing the whole system and the absorber before the system operates, and closing all valves. The degassed brine is added into an evaporator 3, the evaporation temperature is controlled to 15 ℃, a first valve 13 is opened, the evaporator 3 is communicated with a first adsorber 1, the brine in the evaporator 3 is continuously evaporated to take away heat, low-temperature cooling water can be obtained through a heat exchange coil 6, and meanwhile, the brine in the evaporator 3 is continuously concentrated. After the adsorption time reaches 2.5h, the first valve 13 is closed, and the first adsorber 1 is exposed to the sun. When the temperature of the first adsorber 1 reaches 60 ℃, the valve third valve 15 and the condenser valve 17 are opened, and the water vapor desorbed from the first adsorber 1 enters the condenser 7 to be condensed to obtain purified fresh water, and flows into the direct drinking water storage tank 18 to be stored. Simultaneously, the second valve 14 is opened, the evaporator 3 is connected with the second adsorber 2, the brine in the evaporator 3 is continuously evaporated to take away heat, and the brine is also continuously concentrated. When the half cycle time (adsorption time 2.5h, total time of heating, desorbing and cooling 2.5 h) is reached, the first valve 13, the second valve 14 and the condenser valve 17 are closed, the third valve 15 and the fourth valve 16 are kept in an open state, the first adsorber 1 and the second adsorber 2 are communicated, the quality returning operation is carried out for 1min, and the third valve 15 and the fourth valve 16 are closed after the quality returning operation is finished. Cooling water with the temperature of 25 ℃ is introduced into copper tubes at the bottom of the first adsorber 1 from the cold/hot water inlet 11 to cool the first adsorber 1. The second adsorber 2 is exposed to the sun. When the first adsorber 1 reaches 30 ℃, the second adsorber 2 reaches 60 ℃, and then the cooling water is stopped from flowing into the first adsorber 1. The first valve 13 is opened, the evaporator 3 is connected with the first adsorber 1, the brine in the evaporator 3 is continuously evaporated to take away heat, and the brine is also continuously concentrated. Simultaneously, the fourth valve 16 is opened, the water vapor desorbed from the second adsorber 2 enters the condenser 7 to be condensed to obtain purified fresh water, and flows into the direct drinking water storageStored in tank 18. When the preset half cycle time is reached, the first valve 13, the second valve 14 and the condenser valve 17 are closed, the third valve 15 and the fourth valve 16 are kept in an open state, the first adsorber 1 and the second adsorber 2 are connected for 1min of returning to the quality, and after the returning to the quality is finished, the third valve 15 and the fourth valve 16 are closed. 113.6g/kg of the product are obtained after the end of the process ads Purifying fresh water, and the refrigerating capacity reaches 278.3kJ/kg.
Example 2
The specific operation procedure was the same as in example 1; when the adsorbent is a foam nickel solidified silica gel composite adsorbent coated with 3% GrO photo-thermal material coating, the mass percentage of silica gel is 50%, the mass percentage of foam nickel is 47%, the solid-liquid ratio of silica gel to brine is 2.2, the evaporation temperature is 15 ℃, and the cycle time is 5 hours, 95.6g/kg can be obtained ads Purifying fresh water, and the refrigerating capacity reaches 234.2kJ/kg.
Example 3
The specific operation procedure was the same as in example 1; when the adsorbent is a foamed aluminum cured silica gel composite adsorbent coated with a carbon nano tube photo-thermal material coating, the mass percentage of the carbon nano tube photo-thermal material coating material is 5%, the solid-liquid ratio of the adsorbent to brine is 4, the mass percentage of silica gel is 64%, the mass percentage of foamed aluminum is 31%, the solid-liquid ratio of the silica gel to brine is 2.2, the evaporation temperature is 15 ℃, and 104.4g/kg can be obtained after the circulation time is 5 hours ads Purifying fresh water, and the refrigerating capacity reaches 255.8kJ/kg.
Example 4
The specific operation procedure was the same as in example 1; when the foam copper coated with the nano metal photo-thermal material coating is solidified into MIL-101 (Cr) composite adsorbent, the mass percentage of the nano metal photo-thermal material coating material is 1%, the mass percentage of MIL-101 (Cr) is 37%, the mass percentage of foam copper is 62%, the solid-liquid ratio of MIL-101 (Cr) and brine is 1.3, the evaporation temperature is 15 ℃, and 322.8g/kg can be obtained after the circulation time is 5 hours ads Purifying fresh water, and the refrigerating capacity reaches 790.9kJ/kg.
Example 5
The specific operation procedure was the same as in example 1; the adsorbent is foam copper solidified MIL-101 (Cr) composite adsorption coated with GO photo-thermal material coatingIn the preparation process, the mass percentage of the GO photo-thermal material coating material is 1%, the mass percentage of MIL-101 (Cr) is 37%, the mass percentage of the foam copper is 62%, the solid-liquid ratio of MIL-101MIL-101 (Cr) to brine is 1.3, the evaporation temperature is 20 ℃, and 429.3g/kg can be obtained after the circulation time is 5 hours ads Purifying fresh water, and the refrigerating capacity reaches 1051.8kJ/kg.
Example 6
The specific operation procedure was the same as in example 1; when the foam copper solidified SAPO-34 composite adsorbent coated with the GO photo-thermal material coating is prepared by mixing, by mass, 0.5% of the GO photo-thermal material coating material, 58.5% of the SAPO-34, 41% of the foam copper, and 2.0% of the solid-liquid ratio of the SAPO-34 to the brine, wherein the evaporation temperature is 15 ℃, and 53.3g/kg of the foam copper can be obtained after the circulation time is 5 hours ads Purifying fresh water, and the refrigerating capacity reaches 130.6kJ/kg.
Example 7
The specific operation procedure was the same as in example 1; when the adsorbent is a foamy copper solidified SAPO-34 composite adsorbent coated with a carbon nano tube photo-thermal material coating, the mass percentage of the carbon nano tube photo-thermal material coating material is 1%, the mass percentage of the SAPO-34 is 58%, the mass percentage of the foamy copper is 41%, the solid-liquid ratio of the SAPO-34 and brine is 2.0, the evaporation temperature is 10 ℃, and 50.7g/kg of the foamy copper can be obtained after the circulation time is 5 hours ads Purified fresh water with the refrigerating capacity of 124.1kJ/kg.
Example 8
The specific operation procedure was the same as in example 1; the adsorbent is foam copper solidified CuSO coated with GO photo-thermal material coating 4 When the adsorbent is compounded, the mass percentage of the GO photo-thermal material coating material is 1%, and the mass percentage of the CuSO 4 44% by mass of copper foam 55% by mass of CuSO 4 The solid-liquid ratio with brine is 1.7, the evaporation temperature is 15 ℃, and 382.5g/kg can be obtained after the circulation time is 5 hours ads Purifying fresh water, and the refrigerating capacity reaches 937.1kJ/kg.
Example 9
The specific operation procedure was the same as in example 1; when the adsorbent is a foam copper cured silica gel composite adsorbent coated with a GO photo-thermal material coating, the mass percentage of the GO photo-thermal material coating material is 1%, and the mass percentage of the silica gel is as follows55 percent of foam copper, 44 percent of foam copper, 2.2 percent of solid-to-liquid ratio of silica gel and brine, the evaporation temperature is 20 ℃, and 130.0g/kg of foam copper can be obtained after the circulation time is 5 hours ads Purifying fresh water, and the refrigerating capacity reaches 318.5kJ/kg.
Example 10
The specific operation procedure was the same as in example 1; when the adsorbent is foamed copper solidified silica gel coated with a perovskite photo-thermal material coating, the mass percentage of the perovskite photo-thermal material coating material is 1%, the mass percentage of the silica gel is 55%, the mass percentage of the foamed copper is 44%, the solid-liquid ratio of the silica gel to brine is 2.2, the evaporation temperature is 15 ℃, and 67.2g/kg can be obtained after 2 hours of circulation time ads Purified fresh water with refrigerating capacity up to 164.6kJ/kg.
Example 11
The specific operation procedure was the same as in example 1; when the adsorbent is foam copper solidified silica gel coated with a carbon black photo-thermal material coating, the evaporation temperature is 15 ℃, the mass percentage of the carbon black photo-thermal material coating material is 1%, the mass percentage of the silica gel is 55%, the mass percentage of the foam copper is 44%, and 133.2g/kg can be obtained after 12 hours of circulation time ads Purified fresh water, and the refrigerating capacity reaches 326.3kJ/kg.
Comparative example 1
The specific operation procedure was the same as in example 1; when the adsorbent is coated with the silica gel composite adsorbent coated with the GO photo-thermal material, the mass percentage of the GO photo-thermal material coating material is 0.5%, the mass percentage of the silica gel is 99.5%, the solid-liquid ratio of the silica gel to the brine is 2.2, the evaporation temperature is 15 ℃, and 64.0g/kg can be obtained after the circulation time is 5 hours ads Purifying fresh water, and the refrigerating capacity reaches 161.4kJ/kg.
Comparative example 2
The specific operation procedure was the same as in example 1; when the adsorbent is a foam copper solidified silica gel composite adsorbent, the mass percentage of silica gel is 55%, the mass percentage of foam copper is 45%, the solid-liquid ratio of silica gel to brine is 2.2, the evaporation temperature is 15 ℃, and 39.6g/kg can be obtained after the circulation time is 5 hours ads Purifying fresh water, and the refrigerating capacity reaches 97.0kJ/kg.
Comparative example 3
The specific procedure was the same as in example 1The method comprises the steps of carrying out a first treatment on the surface of the When the adsorbent is a foam nickel solidified silica gel composite adsorbent, the mass percentage of silica gel is 52%, the mass percentage of foam nickel is 48%, the solid-liquid ratio of silica gel to brine is 2.2, the evaporation temperature is 15 ℃, and 36.0g/kg can be obtained after the circulation time is 5 hours ads Purifying fresh water, and the refrigerating capacity reaches 88.2kJ/kg.
Comparative example 4
The specific operation procedure was the same as in example 1; when the adsorbent is foamed aluminum solidified silica gel composite adsorbent, the mass percentage of silica gel is 65%, the mass percentage of foamed aluminum is 35%, the solid-liquid ratio of silica gel to brine is 2.2, the evaporation temperature is 15 ℃, and 38.8g/kg can be obtained after the circulation time is 5 hours ads Purifying fresh water, and the refrigerating capacity reaches 95.1kJ/kg.
The concentrated brine ion concentrations of examples 1-11 and comparative examples 1-4 were tested and the results are shown in Table 1.
Table 1 main ion concentration of brine
The utility model can effectively and rapidly concentrate the brine by using the adsorbent, and the adsorption process is not influenced by the environment such as weather and the like. The adsorbent can be desorbed and regenerated by utilizing low-grade heat sources such as solar energy and the like, and the method has the advantage of low energy consumption.
The concentrations of the main ions of the fresh water of examples 1 to 11 and comparative examples 1 to 4 were tested and the results are shown in Table 2.
TABLE 2 concentration of primary ions in fresh water
According to national standard of drinking mineral water (GB 8537-2018), li + The ion concentration is 0.30-1.34mg/L, which accords with the limit index in the physicochemical standard. The concentration of sodium, potassium, calcium and magnesium ions in the drinking water standard according to the world health organization can meet the requirement of less than 200 mg/L. According to national standard of drinking mineral water (GB 8537-2018), li + The ion concentration is 0.30-1.34mg/L, which accords with the limit index in the physicochemical standard. According to the further stipulation on the aspect of mineral elements of physicochemical standard in the group standard of natural mineral water (suitable for infants), the ion concentration of the fresh water in the table 2 can meet the requirements of less than or equal to 20mg/L of sodium, less than or equal to 10mg/L of potassium, less than or equal to 100mg/L of calcium and less than or equal to 40mg/L of magnesium.
The above is only a preferred embodiment of the present utility model; the scope of the utility model is not limited in this respect. Any person skilled in the art, within the technical scope of the present disclosure, may apply to the present utility model, and the technical solution and the improvement thereof are all covered by the protection scope of the present utility model.
Claims (5)
1. A direct solar adsorption brine concentration refrigeration system, comprising:
an evaporator;
a condenser;
a first adsorber having one end connected to the evaporator and the other end connected to the condenser;
a second adsorber, one end of which is communicated with the evaporator, and the other end of which is communicated with the condenser;
the first absorber and the second absorber are integrated with a solar heat collector, and an adsorbent with direct photo-thermal performance is arranged in the first absorber and the second absorber;
valves are arranged on pipelines which are communicated with the evaporator, the condenser, the first adsorber and the second adsorber, and the valves are also arranged on the condenser;
the adsorbent is a foam metal curing composite adsorbent with a photo-thermal material coating on the surface, and consists of a water absorbing adsorbent, foam metal and a photo-thermal coating material;
the weight percentage of the photo-thermal material is 0.5-5%, the weight percentage of the foam metal is 31-62%, and the weight percentage of the water absorbing adsorbent is 37-64%;
the adsorbent is a foam metal solidified MIL-101 (Cr) composite adsorbent with a photo-thermal material coating on the surface, wherein the mass percentage of MIL-101 (Cr) is 37%, the mass percentage of foam metal is 62%, and the mass percentage of photo-thermal material is 1%;
wherein the photo-thermal material is graphene oxide or nano metal, and the foam metal is foam copper; or (b)
The adsorbent is a foam metal cured silica gel composite adsorbent with a surface coated with a photo-thermal material coating, wherein the mass percentage of silica gel is 55%, the photo-thermal material is carbon black, the mass percentage of the photo-thermal material is 1%, the foam metal is foam copper, and the mass percentage of the foam metal is 44%; or (b)
The adsorbent is foamed metal CuSO with the surface coated with a photo-thermal material coating 4 Composite adsorbent, cuSO 4 The mass percentage of the foam metal is 44%, the mass percentage of the foam metal is 55%, the photo-thermal material is graphene oxide, and the mass percentage of the photo-thermal material is 1%.
2. The direct solar adsorption brine concentrating refrigeration system of claim 1 further comprising auxiliary means;
the auxiliary device is used for cooling or heating the first adsorber and the second adsorber.
3. The direct solar adsorption brine concentrating refrigeration system of claim 2 wherein the auxiliary device has a cold/hot water inlet and a cold/hot water outlet in communication with heat exchange tubes in the first and second adsorbers, respectively, via tubing.
4. A method of using a direct solar absorption brine concentrating refrigeration system according to any one of claims 1 to 3 comprising the steps of:
1) Adding brine into an evaporator, and opening a valve between the evaporator and a first adsorber to perform adsorption;
2) Closing a valve between the evaporator and the first adsorber after the adsorption is completed, opening the valve between the first adsorber and the condenser and the valve on the condenser when the temperature of the first adsorber reaches the desorption temperature, and simultaneously opening the valve between the evaporator and the second adsorber to enable the second adsorber to adsorb;
3) When the second adsorber is completed, closing valves between the evaporator and the first adsorber and between the second adsorber, closing valves on the condenser, opening valves between the first adsorber, the second adsorber and the condenser, enabling the first adsorber to be communicated with the second adsorber for returning the quality, and closing the valves between the first adsorber, the second adsorber and the condenser after the quality returning is completed;
4) And after the first adsorber and the second adsorber reach adsorption and desorption temperatures respectively, opening a valve between the evaporator and the first adsorber, opening a valve between the second adsorber and the condenser and opening a valve on the condenser.
5. The method of claim 4, wherein the auxiliary device heats the desorption water by introducing a heat medium as an auxiliary energy source into the second adsorber when the illumination is insufficient;
the auxiliary device introduces a cooling medium into the first adsorber to cool the first adsorber.
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