CN106517449B - Solution regeneration device capable of improving current efficiency - Google Patents
Solution regeneration device capable of improving current efficiency Download PDFInfo
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- CN106517449B CN106517449B CN201710009533.XA CN201710009533A CN106517449B CN 106517449 B CN106517449 B CN 106517449B CN 201710009533 A CN201710009533 A CN 201710009533A CN 106517449 B CN106517449 B CN 106517449B
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- 230000008929 regeneration Effects 0.000 title claims abstract description 155
- 238000011069 regeneration method Methods 0.000 title claims abstract description 155
- 238000011033 desalting Methods 0.000 claims abstract description 34
- 238000004519 manufacturing process Methods 0.000 claims abstract description 32
- KWGKDLIKAYFUFQ-UHFFFAOYSA-M lithium chloride Chemical compound [Li+].[Cl-] KWGKDLIKAYFUFQ-UHFFFAOYSA-M 0.000 claims description 24
- 238000010612 desalination reaction Methods 0.000 claims description 20
- 230000001172 regenerating effect Effects 0.000 claims description 17
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 14
- 239000003011 anion exchange membrane Substances 0.000 claims description 5
- 239000012528 membrane Substances 0.000 claims description 4
- 238000005341 cation exchange Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 17
- 230000008569 process Effects 0.000 abstract description 13
- 238000007791 dehumidification Methods 0.000 abstract description 10
- 238000004378 air conditioning Methods 0.000 abstract description 9
- 239000000243 solution Substances 0.000 description 223
- 238000000909 electrodialysis Methods 0.000 description 19
- 239000007864 aqueous solution Substances 0.000 description 12
- 239000007789 gas Substances 0.000 description 11
- 229910052736 halogen Inorganic materials 0.000 description 11
- 150000002367 halogens Chemical class 0.000 description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 7
- 150000001447 alkali salts Chemical class 0.000 description 7
- 230000000779 depleting effect Effects 0.000 description 7
- 239000012266 salt solution Substances 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- 230000010287 polarization Effects 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- 238000009792 diffusion process Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003792 electrolyte Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 239000002274 desiccant Substances 0.000 description 2
- 230000005684 electric field Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000003411 electrode reaction Methods 0.000 description 1
- 239000008151 electrolyte solution Substances 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000003014 ion exchange membrane Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 230000007794 irritation Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000013508 migration Methods 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
- 238000010248 power generation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
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- Analytical Chemistry (AREA)
- Molecular Biology (AREA)
- Health & Medical Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Hydrology & Water Resources (AREA)
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- Environmental & Geological Engineering (AREA)
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Abstract
The invention discloses a solution regeneration device capable of improving current efficiency, which comprises a solution consumption loop, a regeneration solution loop and a power supply, wherein the regeneration solution loop comprises a regeneration solution tank and a regeneration chamber of a solution regenerator, an outlet of the regeneration solution tank is connected with an inlet of the regeneration chamber, and an outlet of the regeneration chamber is connected with an inlet of the regeneration solution tank; the consumption solution loop comprises an anode chamber, a cathode chamber and a desalting chamber of the solution regenerator, and a consumption solution tank, a first production tank and a second production tank; an outlet of the consumption solution tank is connected with an inlet of the desalting chamber, an outlet of the desalting chamber is respectively connected with an inlet of the anode chamber and an inlet of the cathode chamber, an outlet of the anode chamber is connected with an inlet of the first production tank, and an outlet of the cathode chamber is connected with an inlet of the second production tank; the anode of the power supply is connected with the anode of the solution regenerator, and the cathode of the power supply is connected with the cathode of the solution regenerator. The regeneration device can realize regeneration of the regeneration solution in the solution dehumidification air-conditioning system, and improve the current efficiency in the regeneration process.
Description
Technical Field
The invention belongs to the technical field of energy storage air conditioning devices and chemical production, and particularly relates to a solution regeneration device capable of improving current efficiency.
Background
In recent years, the problem of energy shortage caused by traditional refrigeration and air conditioning equipment in buildings is becoming more severe, and the energy consumption of a hot and humid environment control system can be remarkably reduced by utilizing a hot and humid independent treatment method, so that the adjustment method of hot and humid independent treatment is receiving wide attention. Among a plurality of heat and humidity independent processing air conditioning systems, the solution dehumidification air conditioning system is a novel air conditioning mode with great potential based on a liquid moisture absorbent dehumidification technology. Electrodialysis is one of the membrane separation techniques. The electrochemical separation process is that under the action of DC electric field, the electrolyte is separated from the solution by using the selective permeability of ion exchange membrane and using potential difference as power. During the operation of the electrodialyser, the concentration of the solution increases in some compartments (concentrating compartments) and decreases in others (depleting compartments). The solution dehumidifying air-conditioning system adopts the dehumidifying agent (lithium chloride solution, calcium chloride solution and lithium bromide solution) which is mostly electrolyte solution, and the regenerating process of the dehumidifying agent is essentially the process of solution concentration. Thus, a novel method for regenerating an electrodialysis solution can be obtained by using the electrodialysis method.
However, the electrode chambers of the electrodialysis regenerator are subjected to polarization reaction and consume polar aqueous solution continuously during operation, so that the polar aqueous solution needs to be replenished in time during the operation of the electrodialysis regenerator. The electrodialysis regenerator realizes the regeneration of the dehumidification solution by transferring solute ions in the desalination chamber to the regeneration chamber, so that the polarization reaction in the electrode chamber does not help the solution regeneration and can cause the waste of polar water solution, thereby increasing the material cost of the electrodialysis regenerator during operation. On the other hand, the polarization reaction of the electrode chamber of the electrodialysis regenerator can generate halogen gas, the halogen gas has strong irritation and toxicity, direct discharge can cause certain harm to the environment, and the treatment of the halogen gas can increase the operation cost of the electrodialysis regenerator. Furthermore, in solution desiccant air conditioning systems, the desiccant solution typically has a relatively high concentration. For example, when a lithium chloride solution is used as the dehumidifying solution, the mass concentration range thereof is usually about 35%. When the traditional electrodialysis regenerator is used for regenerating the dehumidification solution, the difference between the concentration of the solution in the desalination chamber and the concentration of the polar water solution is not large as that of the solution in the regeneration chamber, otherwise, the solute in the solution in the regeneration chamber can migrate to the solution in the adjacent compartment in a large amount due to the large concentration difference, the actual regeneration effect of the electrodialysis regenerator is weakened, and the electrodialysis regenerator has low current efficiency. For example, when a lithium chloride solution is used as a dehumidifying solution, the mass concentration ranges of the solution in the regeneration chamber and the solution in the desalination chamber of the electrodialysis regenerator are both about 35%, and the mass concentration range of the polar water solution is 15-20%, the concentration difference between the solution in the regeneration chamber and the solution in the electrode chamber is about 20%, and the experimental result shows that the current efficiency of the electrodialysis regenerator is only about 50%. This increases the power consumed by the electrodialysis regenerator, but the higher concentration of the solution in the desalination cells and the solution in the electrode cells leads to higher material cost when the electrodialysis regenerator is operated, so the actual electrodialysis regenerator adopts polar aqueous solution with lower concentration. For example, when a lithium chloride solution is used as the dehumidifying solution, the mass concentration of the extremely aqueous solution is in the range of 15 to 20%. I.e., material costs in the operation of the electrodialysis regenerator are reduced at the expense of current efficiency.
Disclosure of Invention
The technical problem is as follows: the invention aims to provide a solution regeneration device capable of improving current efficiency, which realizes regeneration of a regeneration solution in a solution dehumidification air-conditioning system and improves the current efficiency in a regeneration process.
The technical scheme is as follows: to solve the above-mentioned problems, embodiments of the present invention provide a solution regeneration device capable of improving current efficiency, the solution regeneration device including a consumption solution circuit, a regeneration solution circuit, and a power supply, wherein,
the regeneration solution loop comprises a regeneration solution tank and a regeneration chamber of the solution regenerator, an outlet of the regeneration solution tank is connected with an inlet of the regeneration chamber through a first solution pump, and an outlet of the regeneration chamber is connected with an inlet of the regeneration solution tank; the consumption solution loop comprises an anode chamber, a cathode chamber and a desalting chamber of the solution regenerator, and a consumption solution tank, a first production tank and a second production tank; an outlet of the consumption solution tank is connected with an inlet of a desalting chamber through a second solution pump, an outlet of the desalting chamber is respectively connected with an inlet of an anode chamber and an inlet of a cathode chamber, an outlet of the anode chamber is connected with an inlet of a first production tank, and an outlet of the cathode chamber is connected with an inlet of a second production tank; the anode of the power supply is connected with the anode of the solution regenerator, and the cathode of the power supply is connected with the cathode of the solution regenerator.
Preferably, the solution regenerator is sequentially provided with an anode, an anode chamber, a desalting chamber, a regenerating chamber, a cathode chamber and a cathode, an anion exchange membrane is arranged between the anode chamber and the desalting chamber, a cation exchange membrane is arranged between the desalting chamber and the regenerating chamber, and an anion exchange membrane is arranged between the regenerating chamber and the cathode chamber.
Preferably, the power supply is a direct current power supply.
Preferably, the mass concentration of the consumed solution flowing out of the desalting chamber is 2 to 5 percent lower than that of the regeneration solution flowing into the regeneration chamber; the mass concentration of the consumption solution flowing into the desalting chamber is less than or equal to the mass concentration of the regeneration solution flowing into the regeneration chamber.
As a preferable example, the solution in the consumption solution tank is a consumption solution with a mass concentration of 35%; the solution in the regeneration solution tank is a regeneration solution with the mass concentration of 35%; the mass concentration of the regeneration solution flowing into the regeneration chamber is 35%, and the mass concentration of the regeneration solution flowing out of the regeneration chamber is 37-40%; the mass concentration of the consumed solution flowing into the desalting chamber is 35%, and the mass concentration of the consumed solution flowing out of the desalting chamber is 30-33%.
As a preferred example, the consumption solution is a lithium chloride or lithium bromide solution, and the regeneration solution is a lithium chloride or lithium bromide solution.
Has the advantages that: compared with the prior art, the embodiment of the invention has the following beneficial effects:
in the regeneration device of the embodiment of the invention, the outlet of the desalting chamber of the solution regenerator is respectively connected with the inlet of the anode chamber of the solution regenerator and the inlet of the cathode chamber of the solution regenerator, the consumed solution with reduced mass concentration in the desalting chamber is used for supplying the electrode chamber of the solution regenerator, and the mass concentration of the consumed solution in the anode chamber and the cathode chamber is lower than the mass concentration of the regeneration solution in the regeneration solution tank 2~5%. This improves the current efficiency of the solution regeneration device and reduces the energy consumption of the solution regeneration device. Meanwhile, halogen gas, hydrogen and basic salt solution which are needed in the chemical field and generated by the polarization reaction in the electrode chamber are collected by the inlets of the first production tank and the second production tank, so that unnecessary waste of polar aqueous solution in the electrode chamber is avoided, and the operation cost of halogen gas treatment is saved.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention.
The figure has the following components: the device comprises a solution regenerator 1, an anode chamber 101, an anode chamber inlet 1011, an anode chamber outlet 1012, a cathode chamber 102, a cathode chamber inlet 1021, a cathode chamber outlet 1022, a regeneration chamber 103, a regeneration chamber inlet 1031, a regeneration chamber outlet 1032, a desalination chamber 104, a desalination chamber inlet 1041, a desalination chamber outlet 1042, an anode 105, a cathode 106, a regeneration solution tank 2, a regeneration solution tank outlet 201, a regeneration solution tank inlet 202, a consumption solution tank 3, a consumption solution tank outlet 301, a consumption solution tank inlet 302, a first production tank 4, a first production tank inlet 401, a second production tank 5, a second production tank inlet 501, a power supply 6, a first solution pump 7 and a second solution pump 8.
Detailed Description
The technical solution of the embodiment of the present invention is further described below with reference to the accompanying drawings.
As shown in fig. 1, a solution regeneration apparatus capable of improving current efficiency according to an embodiment of the present invention includes a consumption solution circuit, a regeneration solution circuit, and a power supply 6. The regeneration solution circuit comprises a regeneration chamber 103 of the solution regenerator 1 and a regeneration solution tank 2, the regeneration solution tank outlet 201 being connected to a regeneration chamber inlet 1031 via a first solution pump 7, and a regeneration chamber outlet 1032 being connected to a regeneration solution tank inlet 202. The spent solution circuit comprises an anode chamber 101, a cathode chamber 102 and a desalination chamber 104 of the solution regenerator 1, and a spent solution tank 3, a first production tank 4 and a second production tank 5; the outlet 301 of the consumption solution tank is connected with the inlet 1041 of the desalting chamber through a second solution pump 8, the outlet 1042 of the desalting chamber is respectively connected with the inlet 1011 of the anode chamber and the inlet 1021 of the cathode chamber, the outlet 1012 of the anode chamber is connected with the inlet 401 of the first production tank, and the outlet 1022 of the cathode chamber is connected with the inlet 501 of the second production tank. The positive electrode of the power source 6 is connected to the anode 105 of the solution regenerator 1, and the negative electrode of the power source 6 is connected to the cathode 106 of the solution regenerator 1.
In the apparatus of the above embodiment, the same solution regenerator 1 is used for both the spent solution circuit and the regenerated solution circuit. The solution regenerator 1 is provided with an anode 105, an anode chamber 101, a desalting chamber 104, a regenerating chamber 103, a cathode chamber 102 and a cathode 106 in sequence. Preferably, the power supply 6 is a dc power supply.
In the operation of the apparatus of the above embodiment, in the regeneration solution circuit, the regeneration solution is pressurized from the regeneration solution tank 2 into the regeneration chamber 103 of the solution regenerator 1 by the first solution pump 7. After the mass transfer process between the regeneration solution and the consumption solution in the desalting chamber 104, the concentration is increased and the regeneration solution is changed from a dilute solution to a concentrated solution; the concentrated solution then flows back into the regeneration solution tank 2, thereby completing a closed circulation of the regeneration solution.
For the spent solution circuit, the spent solution is pressurized from the spent solution tank 3 into the depletion chamber 104 of the solution regenerator by the second solution pump 8. In the desalting chamber 104, after the mass transfer process between the consumed solution and the regeneration solution in the regeneration chamber 103, the concentration is reduced to become a dilute solution; then the dilute solution enters the anode chamber 101 and the cathode chamber 102, and the polarization reaction is carried out in the anode chamber and the cathode chamber by controlling the power supply 6, the polar aqueous solution in the anode chamber 101 reacts to generate halogen gas, the halogen gas is discharged into the first production tank 4, the polar aqueous solution in the cathode chamber 102 reacts to generate hydrogen and basic salt solution, and the hydrogen and the basic salt solution are discharged into the second production tank 5, thereby completing the open circulation of the consumed solution. Through setting up first production tank 4 and second production tank 5, collect halogen gas, hydrogen and basic salt solution, can regard as the material for corresponding chemical industry enterprise.
In the apparatus of the above embodiment, preferably, the mass concentration of the consumption solution flowing out of the desalination chamber 104 is 2 to 5% lower than the mass concentration of the regeneration solution flowing into the regeneration chamber 103; the mass concentration of the spent solution flowing into the depleting compartment 104 is less than or equal to the mass concentration of the regeneration solution flowing into the regeneration compartment 103. The mass concentration of the consumed solution flowing out of the desalting chamber 104 is 2-5% less than that of the regenerated solution flowing into the regeneration chamber 103, so that the current efficiency can be improved, and the energy consumption can be reduced. For example, the solution in the spent solution tank 3 is a spent solution having a mass concentration of 35%; the solution in the regeneration solution tank 2 is a regeneration solution having a mass concentration of 35%. The mass concentration of the regeneration solution flowing into the regeneration chamber 103 is 35%, and the mass concentration of the regeneration solution flowing out of the regeneration chamber 103 is 37 to 40%. The mass concentration of the consumed solution flowing into the desalting chamber 104 is 35%, and the mass concentration of the consumed solution flowing out of the desalting chamber 104 is 30-33%. The consumption solution is lithium chloride or lithium bromide solution, and the regeneration solution is lithium chloride or lithium bromide solution.
In the apparatus of the above embodiment, the anode chamber 101 and the cathode chamber 102 are supplied with the use of the depleted solution having a reduced concentration in the depletion chamber 104. Structurally, the consumption solution with the reduced concentration in the desalting chamber 104 is used for supplying the anode chamber 101 and the cathode chamber 102, so that an electrode aqueous solution tank is omitted from the regeneration device, extra electrode aqueous solution circulation is not needed, the material cost of the regeneration device during operation is greatly reduced, and the device structure is simplified.
Functionally, the mass concentration of the spent solution entering the desalination chamber is slightly higher than the mass concentration of the spent solution exiting the desalination chamber. This results in a very low mass concentration of the polar aqueous solution compared to the mass concentration of the regeneration solution in the regeneration chamber and the mass concentration of the depleting solution in the depleting chamber, e.g., 2~5%. This reduces the detrimental migration of solutes in the regeneration solution in the regeneration chamber into the solution in the adjacent compartment, thereby improving the current efficiency of the solution regeneration device and reducing the energy consumption of the entire device.
In the solution regeneration device of this embodiment, under the action of the dc electric field, the anions and cations in the solution migrate to the anode and the cathode, and through the action of the cation exchange membrane and the anion exchange membrane, the concentration of the solution in the regeneration chamber 103 is increased, and the concentration of the solution in the desalination chamber 104 is decreased, which is to say that substantially part of the solute in the solution in the desalination chamber 104 is transferred to the solution in the regeneration chamber 103. Therefore, theoretically, the solution in the regeneration chamber 103 has more solute, and the solution in the desalination chamber 104 has less solute, so that the concentration of the solution in the regeneration chamber 103 increases, and the concentration of the solution in the desalination chamber 104 decreases. Since the solution dehumidification air conditioner requires that the mass concentration of the dehumidification solution be 37 to 40%, the mass concentration of the solution in the regeneration chamber 103 is adjusted by adjusting the supply current of the power supply 6. The larger the current, the more the solution concentration in the regeneration chamber 103 increases, so the mass concentration of the regeneration solution flowing out from the regeneration chamber 103 is ensured to be 37 to 40% by adjusting the current. When the mass concentration of the regeneration solution flowing out of the regeneration chamber 103 is 37-40%, the mass concentration of the consumption solution flowing out of the desalination chamber 104 is 30-33% correspondingly.
An example is illustrated below.
The regeneration solution is a lithium chloride solution. The regeneration solution is a dilute solution when flowing out of the regeneration solution tank 2, and the mass concentration is 35%. The regeneration solution flows from the regeneration solution tank 2 into the regeneration chamber 103 by the first solution pump 7. After the mass transfer process between the regeneration solution and the consumed solution in the desalting chamber 104, the concentration is increased to form a concentrated solution with the mass concentration of 37 to 40 percent, and the concentrated solution flows out of the regeneration chamber 103 and returns to the regeneration solution tank 2.
The consuming solution is a lithium chloride solution. The spent solution is fed into the spent solution tank 3 through a spent solution tank inlet 302. The consumed solution at this time was a dilute solution having a mass concentration of 35%. The spent solution is flowed from the spent solution tank 3 into the desalination chamber 104 by the second solution pump 8. After the mass transfer process between the consumed solution and the regeneration solution in the regeneration chamber 103, the concentration is reduced to become a dilute solution with the mass concentration of 30 to 33 percent. That is, the mass concentration of the spent solution as it flows into the depleting compartment 104 is greater than the mass concentration as it flows out of the depleting compartment 104 by a difference of 2~5%. The spent solution flows out of the depleting compartment 104 into the anode and cathode compartments 101 and 102. The mass concentration of the depleted solution in the anode 101 and cathode 102 chambers is less than the mass concentration of the regeneration solution in the regeneration chamber 103 and less than the mass concentration of the depleted solution in the depletion chamber 104. By controlling the power supply 6, polarization reactions occur in the anode and cathode chambers. In this process, concentration diffusion of the electrolyte occurs in addition to two main processes of ionic electromigration and electrode reaction. Since the average concentration of the regeneration solution in the regeneration chamber 103 is higher than the mass concentration of the consumption solution in the desalination chamber 104, and the average mass concentration of the consumption solution in the desalination chamber is higher than the mass concentration of the solution in the two electrode chambers. Under the action of the concentration difference, the electrolyte can diffuse from the high-concentration compartment to the low-concentration compartment, and the diffusion speed is increased along with the increase of the concentration difference. This process reduces the concentration of the regeneration solution in the regeneration chamber 103, which has a negative effect on the regeneration process of the regeneration device, thereby reducing the regeneration effect of the regeneration device under the same current condition, reducing the current efficiency of the regeneration device, and increasing the energy consumption when the regeneration device regenerates the same solution. Therefore, compared with the concentration difference of about 20% in the traditional electrodialysis regenerator, the concentration difference between the electrode chamber and the regeneration chamber is reduced by the regeneration device provided by the embodiment of the invention, and only 2~5% is provided, so that the concentration difference diffusion in the regeneration process is weakened, the current efficiency of the regeneration device is improved, and the energy consumption of the device is reduced.
In the apparatus of the above embodiment, the aqueous polar solution in the anode chamber 101 reacts to generate halogen gas, the halogen gas is discharged into the first production tank 4, the aqueous polar solution in the cathode chamber 102 reacts to generate hydrogen gas and basic salt solution, and the hydrogen gas and the basic salt solution are discharged into the second production tank 5. The first production tank 4 and the second production tank 5 are used for collecting electrode aqueous solution reaction products, so that the environmental pollution caused by direct elimination is avoided. The collector aqueous solution reaction products of the first production tank 4 and the second production tank 5 can be used as materials in the chemical field, and waste recycling is achieved.
The device of the embodiment can stably and efficiently regenerate the dehumidifying solution under the high-temperature and high-humidity weather condition, can be driven by solar photovoltaic power generation, and is particularly suitable for enterprise buildings for producing halogen gas, hydrogen or basic salt solution. Meanwhile, the device can also utilize low-price electricity at night valley to store energy, so that the peak-valley difference of the power load is relieved, and the purpose of improving the economy of the system is achieved. In addition, the device can also obtain high-concentration dehumidification solution for the field of deep dehumidification.
The foregoing illustrates and describes the principles, general features, and advantages of the present invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are intended to further illustrate the principles of the invention, and that various changes and modifications may be made without departing from the spirit and scope of the invention, which is also intended to be covered by the appended claims. The scope of the invention is defined by the claims and their equivalents.
Claims (6)
1. A solution regenerating device capable of improving current efficiency, characterized in that the regenerating device comprises a consuming solution circuit, a regenerating solution circuit and a power supply (6), wherein,
the regeneration solution loop comprises a regeneration solution tank (2) and a regeneration chamber (103) of the solution regenerator (1), an outlet (201) of the regeneration solution tank is connected with an inlet (1031) of the regeneration chamber through a first solution pump (7), and an outlet (1032) of the regeneration chamber is connected with an inlet (202) of the regeneration solution tank;
the consumption solution loop comprises an anode chamber (101), a cathode chamber (102) and a desalting chamber (104) of the solution regenerator (1), and a consumption solution tank (3), a first production tank (4) and a second production tank (5); an outlet (301) of the consumption solution tank is connected with an inlet (1041) of a desalting chamber through a second solution pump (8), an outlet (1042) of the desalting chamber is respectively connected with an inlet (1011) of an anode chamber and an inlet (1021) of a cathode chamber, an outlet (1012) of the anode chamber is connected with an inlet (401) of a first production tank, and an outlet (1022) of the cathode chamber is connected with an inlet (501) of a second production tank; the mass concentration of the consumed solution flowing out of the desalting chamber (104) is 2 to 5 percent lower than that of the regeneration solution flowing into the regeneration chamber (103);
the anode of the power supply (6) is connected with the anode (105) of the solution regenerator (1), and the cathode of the power supply (6) is connected with the cathode (106) of the solution regenerator (1).
2. The solution regenerating device capable of improving current efficiency according to claim 1, wherein the solution regenerator (1) is provided with an anode (105), an anode chamber (101), a desalting chamber (104), a regenerating chamber (103), a cathode chamber (102) and a cathode (106) in sequence, an anion exchange membrane is provided between the anode chamber (101) and the desalting chamber (104), a cation exchange membrane is provided between the desalting chamber (104) and the regenerating chamber (103), and an anion exchange membrane is provided between the regenerating chamber (103) and the cathode chamber (102).
3. The solution regenerating device capable of improving current efficiency according to claim 1, characterized in that the power source (6) is a direct current power source.
4. The solution regeneration device capable of improving current efficiency according to claim 1, wherein the mass concentration of the consumption solution flowing into the desalination chamber (104) is less than or equal to the mass concentration of the regeneration solution flowing into the regeneration chamber (103).
5. The solution regenerating arrangement capable of improving current efficiency according to any of the claims 1 to 4, characterized in that the solution in the consuming solution tank (3) is a consuming solution with 35% mass concentration; the solution in the regeneration solution tank (2) is a regeneration solution with the mass concentration of 35%;
the mass concentration of the regeneration solution flowing into the regeneration chamber (103) is 35 percent, and the mass concentration of the regeneration solution flowing out of the regeneration chamber (103) is 37 to 40 percent;
the mass concentration of the consumed solution flowing into the desalting chamber (104) is 35 percent, and the mass concentration of the consumed solution flowing out of the desalting chamber (104) is 30 to 33 percent.
6. The apparatus for regenerating a solution for improving current efficiency as set forth in claim 5, wherein said consumption solution is a lithium chloride or lithium bromide solution, and said regeneration solution is a lithium chloride or lithium bromide solution.
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| CN106517449B (en) * | 2017-01-06 | 2022-10-04 | 南京工业大学 | Solution regeneration device capable of improving current efficiency |
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