CN104001342B - A kind of vacuum atomizing flash distillation water separation device for salting liquid - Google Patents
A kind of vacuum atomizing flash distillation water separation device for salting liquid Download PDFInfo
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- CN104001342B CN104001342B CN201410248369.4A CN201410248369A CN104001342B CN 104001342 B CN104001342 B CN 104001342B CN 201410248369 A CN201410248369 A CN 201410248369A CN 104001342 B CN104001342 B CN 104001342B
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Abstract
The invention discloses a kind of vacuum atomizing flash distillation water separation device for salting liquid, comprise evaporimeter, adsorbent bed, condenser, hot-water heating system and cooling water system; Hot-water heating system comprises boiler and heat exchanger; Cooling water system comprises cooling water tank and cooling tower; Evaporimeter inside is provided with dividing plate, and its epimere is vacuum chamber, and hypomere is hot hydroecium, is also provided with the heat pipe group through dividing plate.Hot hydroecium is connected with boiler and heat exchanger; Vacuum chamber is connected with adsorbent bed; Adsorbent bed is connected with condenser, cooling tower, heat exchanger, boiler and cooling water tank; Condenser is connected with cooling tower and cooling water tank; Pipeline between boiler and hot hydroecium and adsorbent bed is provided with heat-exchanger pump; Pipeline between cooling water tank and condenser and adsorbent bed is provided with cooling water pump.Vacuum atomizing flash distillation water separation device for salting liquid provided by the invention, have capacity usage ratio high, less demanding to raw water quality, to advantages such as driving heat source temperature requirement are low, easy to control.
Description
Technical field
The present invention relates to a kind of low-grade heat source and utilize technique device, particularly, relate to a kind of based on solid absorption driving and the salting liquid vacuum atomizing flash distillation water separation device utilizing heat pipe intensified heat transfer.
Background technology
In recent years, solution dehumidification technology obtains and develops faster, and solution dehumidification system can adopt low-temperature heat source to drive, and utilizes the salting liquid possessing strong wettability power to carry out caloic exchange with humid air in dehumidifier, and then reaches the object of air dewetting.Which overcome the problem that freeze drying consumes high-grade energy, high energy consumption and contaminated environment.Dehumidifier and regenerator are the most important building blocks of solution dehumidifying air-conditioning system.The heat and mass transfer performance of regenerator directly has influence on the effect on moisture extraction of whole process.The regenerator configuration form of current solution dehumidification system is roughly divided into following several: interior pattern of fever regenerator, heat insulation-type regenerator, solar energy heating type regenerator, vaporation-type regenerator.
Wherein, interior pattern of fever regenerator is compensated because moisture in solution evaporates the heat taken away by external heat source, and maintaining actified solution has certain temperature, is similar to isothermal regeneration, ensure that the pressure differential power of regenerative process, improve regeneration efficiency.As shown in Figure 1.Weak solution to be sent into successively in preheater, heater by solution pump by bottom and is carried out preheating, improve solution water steam surface steam pressure, then spray on the packing layer of regenerator, contact with air, in solution, steam is exchanged by caloic and is pulled away, due to moisture evaporation endothermic, solution temperature reduces, and the solution circulation after cooling enters heater and heats.Although cyclic process ensure that the regeneration temperature that solution is certain, owing to still adopting air contact zones to walk the method for steam, the lifting of regeneration efficiency is still limited.
In a word, although interior pattern of fever and the application of solar energy heating formula are comparatively extensively, itself is Shortcomings still, and as apparatus and process is comparatively complicated, regeneration efficiency is restricted etc.Therefore while improving existing regenerator type, also need to study new and effective regenerator, in order to improve the problems such as system regeneration efficiency.
In field of sea water desalting technology, conventional method for desalting seawater has counter-infiltration, multistage flash evaporation, multi-effect distilling and pressure steam distillation, and rear three belongs to thermal distillation method.Counter-infiltration system is driven by electric energy/mechanical energy, and in membrane module performance, Energy Recovery Technology etc., obtained tremendous development in recent years, making water cost declines to a great extent, and it produces water capacity and has accounted for more than 50% of desalinization total capacity.Thermal distillation method for desalting seawater is mainly used in electricity-water coproduction at present, namely utilizes the heat energy of power plant's lower temperature to produce fresh water, and in addition, the method is very suitable for effective utilization of industrial afterheat recovery and the low-grade heat source such as solar thermal energy, geothermal energy.
Multi-stage flash evaporation technology based on flash distillation theory is applied for many years in field of seawater desalination, and Fig. 2 is its single-stage schematic diagram.Upper level seawater enters this grade of flash distillation by throttle nozzle, and the moisture flashed off is by the condensation tube bank condensation on top, and condensate liquid is collected by fresh water dish and discharged.
Can see from above introduction, solution dehumidification technology is to improve cocnentration factor for goal in research, and multistage flash evaporation seawater desalting improves water generation ratio for research direction, although both objects are different, but its core essence is completely the same, namely by heat-driven and vacuum degree control, the moisture as far as possible fast and efficiently in separation solution.And the fundamental driving force that moisture is constantly separated is the initial flash temperature of solution and the difference of cooling water temperature, namely under certain vacuum degree condition, the speed of cooling water collateral coagulation steam determines the evaporation rate of moisture in solution, and rate of set depends primarily on cooling water temperature.
With regard to condensation process, there are 2 deficiencies: (1) condensation process is by the latent heat of condensation of sensible heat " neutralization " steam of cooling water, and efficiency is very low, and condensation process steam quasi-equilibrium pressure is higher, close to 8 ~ 50kPa, reduce the degree of superheat of solution inlet, constrain evaporation ends evaporation efficiency; (2) because of the temperature reference of conventional cooling water, (seawater desalination system cooling water mainly adopts seawater, general about 25 DEG C, dehumidification solution regeneration then adopts cooling tower cooling water, general about 32 DEG C), low-grade heat source range can be utilized to be restricted, when such as adopting 60 DEG C of solution multistage flash evaporation regeneration, both temperature difference only have 28 DEG C, can arrange progression and be restricted.
With regard to solution flash process, there are 2 deficiencies: (1) this be the evaporation of face, disengagement area is limited; (2) continuing along with moisture evaporation, bulk solution temperature reduces fast, and namely the degree of superheat reduces even to disappear, and its evaporation intensity also weakens thereupon.
Obviously, for the solution being in evaporation process provides enough heats to become the key factor keeping its evaporation intensity, the coagulability that condenser matches simultaneously is also the important step that this process can continue to carry out.Current no matter multistage flash evaporation or the desalination technology of low temperature multiple-effect distillation, all adopt step by step transformation to adapt to the demand of seawater or boiling temperature stepped change, although this design is the Multi-class propagation based on heat, but the caving-in bash that single-stage evaporation amount is limited, therefore raising single-stage evaporation amount and heat utilization rate then can optimize whole system design.
Summary of the invention
The object of this invention is to provide a kind of device for moisture in rapidly and efficiently separated salt solution, overcome existing technical disadvantages, by heat pipe intensified heat transfer, solid absorption drive, these three kinds of combine with technique of vacuum atomizing flash distillation, have capacity usage ratio high, less demanding to raw water quality, to advantages such as driving heat source temperature requirement are low, easy to control.
In order to achieve the above object, the invention provides a kind of vacuum atomizing flash distillation water separation device for salting liquid, wherein, this device comprises evaporimeter, adsorbent bed, condenser, hot-water heating system and cooling water system; Described hot-water heating system comprises the boiler and heat exchanger that are connected by pipeline; Described cooling water system comprises the cooling water tank and cooling tower that are connected by pipeline; Described evaporimeter inside is provided with dividing plate, and is divided into closed two sections by described dividing plate, and epimere is vacuum chamber, and hypomere is hot hydroecium; Described evaporimeter inside is also vertically provided with heat pipe group, and described heat pipe group is through dividing plate, and the condensation segment of heat pipe group and evaporator section lay respectively in described vacuum chamber and hot hydroecium; Be provided with pipeline below described hot hydroecium to be connected with boiler and heat exchanger respectively; Be provided with pipeline above described vacuum chamber to be connected with adsorbent bed; Described adsorbent bed is also connected with condenser, cooling tower, heat exchanger, boiler and cooling water tank respectively by pipeline; Described condenser is also connected with cooling tower and cooling water tank respectively by pipeline; Pipeline between described boiler and hot hydroecium and adsorbent bed is provided with heat-exchanger pump, hot water in boiler can be pumped, then flow through hot hydroecium and adsorbent bed respectively, then get back to described boiler after described heat exchanger is heated by low-temperature heat source, complete circulation; Pipeline between described cooling water tank and condenser and adsorbent bed is provided with cooling water pump, the cold water in cooling water tank can be pumped, then flows through condenser and adsorbent bed respectively, then get back to described cooling water tank after cooling tower cooling, complete circulation.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, is provided with atomization sprayer above described internal vacuum chamber; Described atomization sprayer is connected with the weak solution pump being arranged on evaporimeter outside by pipeline; Described vacuum chamber side is also provided with an entrance, and be provided with successively on the pipeline outside from this porch vacuum valve, drier and and vavuum pump; Drier Absorbable rod residual water vapor, ensures that the normal safe of vavuum pump runs; Described vacuum chamber bottom is provided with outlet, is connected with concentrated solution case from the pipeline that this exit is outside, is provided with the first drain valve between described concentrated solution case and this outlet.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, the pipeline be connected with adsorbent bed above described vacuum chamber is provided with valve.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, the pipeline between described adsorbent bed and boiler and cooling water tank is respectively equipped with valve; Described adsorbent bed and the pipeline between condenser, cooling tower and heat exchanger are also respectively equipped with valve.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, described condenser inside is provided with condenser coil, water-supporting disc is provided with below it, the opening leading to condenser external is provided with at the bottom part down of this water-supporting disc, be connected with fresh-water tank at this opening part by pipeline, the pipeline between this opening and fresh-water tank is provided with the second drain valve.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, described adsorbent bed adopts two to be one group, and often group comprises the first adsorbent bed and the second adsorbent bed, can increase group number according to vapor flow.Two adsorbent beds are alternately connected with cold water or hot water, to realize adsorption and desorption simultaneously, ensure carrying out continuously of process.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, the first described adsorbent bed and the second adsorbent bed inside are respectively equipped with the first adsorbent bed internal duct and the second adsorbent bed internal duct, and by its respectively all be connected cooling tower, heat exchanger, and cooling water tank, boiler pipeline connection, make can pass into cooling water in the first adsorbent bed internal duct and the second adsorbent bed internal duct to keep adsorption capacity to saturated, and circulate, the low-grade hot water that also can pass into 55-90 DEG C carries out desorption and circulates.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, described heat exchanger adopts shell-and-tube heat exchanger.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, the pipeline between the first described adsorbent bed and the second adsorbent bed and boiler and cooling water tank is provided with circulation of fluid pump.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, described adsorbent bed inside is also provided with can the solid absorbent of adsorb water vapor, and such as silica gel, zeolite etc., its adsorption pressure can reach 1kPa ~ 2kPa.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, the course of work of described device is:
System is vacuumized final vacuum valve v-2 and closes by vavuum pump b-2; Salting liquid through low-grade heat source preheating is pumped to atomization sprayer, becomes fine droplets and by spray to vacuum chamber flash distillation, be full of whole vacuum chamber after atomization; During flash distillation, atomized soln body temperature declines rapidly, but the rapid heat that absorbs elevates the temperature on heat pipe group surface, and the degree of superheat increases, and forms double evaporation-cooling; Now hot intraductal working medium is at upper end condensation heat, is back to lower end under gravity, and absorb heat in hot hydroecium and again evaporate, salting liquid becomes concentrated solution because of moisture flash distillation, by drain valve v-1 is collected into concentrated solution case after gathering bottom vacuum chamber; When flash distillation starts, vacuum indoor pressure sharply increases because of moisture evaporation, utilizes solid absorbent steam to strong adsorption effect, such as silica gel, zeolite etc., its adsorption pressure can reach 1kPa ~ 2kPa, Quick Catch steam, to maintain vacuum; When steam is adsorbed, a large amount of heat of adsorption being released, keeping adsorption capacity by leading to cooling water to adsorbent bed; When absorption is tending towards saturated, passes to the low-grade hot water of 55-90 DEG C to adsorbent bed, desorption is carried out to solid absorbent; The steam produced during desorption, in condenser coil surface condensation, becomes water droplet, drips and accumulates on water-supporting disc, in final inflow fresh-water tank; By valve transfer, make adsorbent bed alternating sorbent desorption, can ensure water separation process continue carry out.Wherein cooling water and hot water are provided by cooling water system hot-water heating system of unifying, and form the Inner eycle closed.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, the heat pipe for thermal conductivity coefficient of described heat pipe group is 10
5the W/ms order of magnitude.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, the driving heat source that described device adopts comes from the low-grade heat source of 55-90 DEG C, comprises solar energy and industrial exhaust heat, used heat etc.
Vacuum atomizing flash distillation water separation device for salting liquid provided by the invention has the following advantages:
1. salting liquid goes out moisture by the method energy quick separating of vacuum flashing, becomes concentrated solution and fresh water.
2. atomization makes solution become fine droplets, greatly can not only increase flash separation face, and obviously can lengthen the suspension time of drop, be conducive to the continuation of flash separation.
3. the thermal conductivity factor of heat pipe is 10
5the W/ms order of magnitude is 10 of copper
3~ 10
4doubly, heat can be supplemented rapidly to the fine droplets of the fast cooling because of flash distillation, keep the degree of superheat even improving drop, form secondary heat absorption evaporation at the tube surface of isothermal, there is higher evaporation rate.
4., by changing topping up working medium and liquid filled ratio, the mode such as be evacuated, and can mate the low-temperature heat source under different temperatures.
5. driving heat source comes from the low-grade heat source of 55-90 DEG C, comprises solar energy and industrial exhaust heat, used heat etc., has fabulous energy-saving effect.
6. its adsorption pressure of high performance adsorbent can reach 1kPa ~ 2kPa, compares the equilibrium partial pressure of cooling water condensation, can significantly improve the degree of superheat of evaporation ends, have higher evaporation rate.
7. suitably regulate salting liquid temperature and the cold water temperature difference can control and regulate vacuum pressure, ensure flash process continue carry out, vavuum pump only uses when manufacturing initial vacuum and getting rid of incoagulable gas.
8. adopt many adsorbent beds to switch, and take backheat measure, the continuation of system cloud gray model can be ensured and improve the thermal efficiency.
9. before vavuum pump, drier is set, prevents the infiltration of a small amount of moisture, ensure vavuum pump security of operation.
10. of many uses, can not only be used for dehumidification regeneration system solution, desalinize seawater, also can waste water, sewage etc. be processed, realize resource regeneration.
Accompanying drawing explanation
Fig. 1 is existing internal heat type regenerator schematic diagram.
Fig. 2 is existing multistage flash evaporation single-stage generalized section.
Fig. 3 is the structural representation of the present invention for the vacuum atomizing flash distillation water separation device of salting liquid.
Fig. 4 is the adsorbent bed partial schematic diagram of the present invention for the vacuum atomizing flash distillation water separation device of salting liquid.
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is further described.
As shown in Figure 3, the vacuum atomizing flash distillation water separation device for salting liquid provided by the invention, comprises evaporimeter 16, adsorbent bed 17, condenser 8, hot-water heating system and cooling water system.
Hot-water heating system comprises the boiler 15 and heat exchanger 14 that are connected by pipeline.Heat exchanger 14 adopts shell-and-tube heat exchanger.
Cooling water system comprises the cooling water tank 13 and cooling tower 11 that are connected by pipeline.
Evaporimeter 16 inside is provided with dividing plate 2, and is divided into closed two sections by dividing plate 2, and epimere is vacuum chamber 5, and hypomere is hot hydroecium 1; Evaporimeter 16 inside is also vertically provided with heat pipe group 4, and heat pipe group 4 is through dividing plate 2, and the condensation segment of heat pipe group 4 and evaporator section lay respectively in vacuum chamber 5 and hot hydroecium 1.
Vacuum chamber 5 inner upper is provided with atomization sprayer 6; Atomization sprayer 6 is connected with the weak solution pump b-1 being arranged on evaporimeter 16 outside by pipeline; Also be provided with an entrance above vacuum chamber 5, and be provided with successively on the pipeline outside from this porch vacuum valve v-2, drier 7 and and vavuum pump b-2; Drier 7 Absorbable rod residual water vapor, ensures normal, the safe operation of vavuum pump b-2, can connect external device (ED) by vavuum pump b-2; Vacuum chamber 5 bottom is provided with outlet, is connected with concentrated solution case 3 from the pipeline that this exit is outside, is provided with the first drain valve v-1 between concentrated solution case 3 and this outlet.
Be provided with pipeline below hot hydroecium 1 to be connected with boiler 15 and heat exchanger 14 respectively; Be provided with pipeline above vacuum chamber 5 to be connected with adsorbent bed 17.The pipeline be connected with adsorbent bed 17 above vacuum chamber 5 is provided with valve v-8 and v-10.
Adsorbent bed 17 is also connected with condenser 8, cooling tower 11, heat exchanger 14, boiler 15 and cooling water tank 13 respectively by pipeline.Adsorbent bed 17 inside is provided with can the solid absorbent of adsorb water vapor, and such as silica gel, zeolite etc., its adsorption pressure can reach 1kPa ~ 2kPa.Adsorbent bed 17 adopts two to be one group, and often group comprises the first adsorbent bed 17 I and the second adsorbent bed 17 II, and can increase group number according to vapor flow, two adsorbent beds 17 are alternately connected with cold water or hot water, to realize adsorption and desorption simultaneously, ensures carrying out continuously of process.First adsorbent bed 17 I and the second adsorbent bed 17 II inside are respectively equipped with the first adsorbent bed internal duct 18 and the second adsorbent bed internal duct 19, and by its respectively all be connected cooling tower 11, heat exchanger 14, and cooling water tank 13, boiler 15 pipeline connection, make can pass into cooling water to keep adsorption capacity to saturated in the first adsorbent bed internal duct 18 and the second adsorbent bed internal duct 19, and circulate, the low-grade hot water that also can pass into 55-90 DEG C carries out desorption and circulates.Pipeline between adsorbent bed 17 and boiler 15 and cooling water tank 13 is provided with circulation of fluid pump b-4.During two switch, the hot and cold water blending flowing of adsorbent bed 17 internal duct, realizes the backheat between two.Pipeline between adsorbent bed 17 and boiler 15 and cooling water tank 13 is respectively equipped with valve v-16, v-18 and v-15, v-17; Adsorbent bed 17 and the pipeline between condenser 8, cooling tower 11 and heat exchanger 14 are also respectively equipped with valve v-9, v-14 and v-7, v-12 and v-6, v-13, shown in Figure 4.
Condenser 8 is also connected with cooling tower 11 and cooling water tank 13 respectively by pipeline.Condenser 8 inside is provided with condenser coil 9, water-supporting disc 10 is provided with below it, be provided with the opening leading to condenser 8 outside at the bottom part down of this water-supporting disc 10, be connected with fresh-water tank 12 at this opening part by pipeline, the pipeline between this opening and fresh-water tank 12 is provided with the second drain valve v-3.Fresh-water tank 12 is also provided with valve v-4 and v-5.Drain valve v-1 and v-3 is normally open valve, by the Energy control of vavuum pump b-2, closes, open draining when vavuum pump b-2 quits work when vavuum pump b-2 opens.
Pipeline between boiler 15 and hot hydroecium 1 and adsorbent bed 17 is provided with heat-exchanger pump b-5, hot water in boiler 15 can be pumped, then flow through hot hydroecium 1 and adsorbent bed 17 respectively, then get back to boiler 15 after heat exchanger 14 is heated by low-temperature heat source, complete circulation.
Pipeline between cooling water tank 13 and condenser and adsorbent bed 17 is provided with cooling water pump b-3, cold water in cooling water tank 13 can be pumped, then flow through condenser 8 and adsorbent bed 17 respectively, then get back to cooling water tank 13 after cooling tower 11 cools, complete circulation.
The course of work of the vacuum atomizing flash distillation water separation device for salting liquid provided by the invention is:
The driving heat source that device adopts comes from the low-grade heat source of 55-90 DEG C, comprises solar energy and industrial exhaust heat, used heat etc.First, system is vacuumized final vacuum valve v-2 and closes by vavuum pump b-2; Salting liquid through low-grade heat source preheating is pumped to atomization sprayer 6, becomes fine droplets and by spray to vacuum chamber 5 flash distillation, be full of whole vacuum chamber 5 after atomization; During flash distillation, atomized soln body temperature declines rapidly, but the rapid heat that absorbs elevates the temperature on heat pipe group 4 surface, and the degree of superheat increases, and forms double evaporation-cooling; The heat pipe for thermal conductivity coefficient of heat pipe group 4 is 10
5the W/ms order of magnitude; Now hot intraductal working medium is at upper end condensation heat, be back to lower end under gravity, absorb heat in hot hydroecium 1 and again evaporate, salting liquid becomes concentrated solution because of moisture flash distillation, by drain valve v-1 is collected into concentrated solution case 3 after gathering bottom vacuum chamber 5; When flash distillation starts, in vacuum chamber 5, pressure sharply increases because of moisture evaporation, utilizes solid absorbent steam to strong adsorption effect, such as silica gel, zeolite etc., its adsorption pressure can reach 1kPa ~ 2kPa, Quick Catch steam, to maintain vacuum; When steam is adsorbed, a large amount of heat of adsorption can be released, lead to cooling water by giving adsorbent bed 17 and keep adsorption capacity; When absorption is tending towards saturated, passes to the low-grade hot water of 55-90 DEG C to adsorbent bed 17, desorption is carried out to solid absorbent; The steam produced during desorption, at condenser coil 9 surface condensation, becomes water droplet, drips and accumulates on water-supporting disc 10, in final inflow fresh-water tank 12; By valve transfer, make the first adsorbent bed 17 I and the second adsorbent bed 17 II alternating sorbent desorption, can ensure water separation process continue carry out.Wherein cooling water and hot water are provided by cooling water system hot-water heating system of unifying, and form the Inner eycle closed.
Embodiment 1
Drain valve v-1, v-3 are normally open valve, and v-4, v-5 are normally close valve, and controlling power supply is vavuum pump b-2, start power supply and light current.
Start-up phase: valve v-7, v-15, v-12, v-17 open, cooling tower 11, cooling water pump b-3, heat-exchanger pump b-5 start, heat exchanger 14 starts to pass into waste heat heat exchange, the first adsorbent bed 17 I and the second adsorbent bed 17 II is made all to be in cryogenic absorption state, and heat pipe group 4 is heated up, internal working medium is by thermal evaporation; Vavuum pump b-2 starts, and now vacuum valve v-2, v-8, v-9, v-10, v-14 opens, and valve v-4, v-5 close.
Pressure change in vacuum chamber 5 is observed by pressure gauge, when vavuum pump b-2 is pumped to close to limiting condition, close vavuum pump b-2 and vacuum valve v-2, v-8, v-9, v-14, open weak solution pump b-1, extract through preheated weak solution, and press-in is contained in the atomization sprayer 6 of vacuum chamber 5 middle and upper part, weak solution is atomized in atomization sprayer 6, flash distillation in spray to vacuum chamber 5, during flash distillation, atomized soln body temperature declines rapidly, but absorb rapidly heat at the tube surface of heat pipe group 4 to elevate the temperature, the degree of superheat increases, and forms double evaporation-cooling.Now hot intraductal working medium is at upper end condensation heat, is back to lower end under gravity, absorbs heat and again evaporate in hot hydroecium 1.The steam flashed off is adsorbed to maintain the vacuum of flash process under the second adsorbent bed 17 II absorption affinity drives, and the concentrated solution after flash distillation is gathered bottom vacuum chamber 5, drains into concentrated solution case 3 by drain valve v-1.
Observed by pressure gauge, when the second adsorbent bed 17 II adsorbance is tending towards saturated, shutoff valve v-10, v-12, v-17, open valve v-8, v-14, v-13, v-18, heat-exchanger pump b-5 starts.
At this moment the start starting stage terminates, and running the first beginning that partly circulates of circulation continuously, is now system mode point A.First adsorbent bed 17 I starts to adsorb the steam flashed off, and the second adsorbent bed 17 II passes into the upper high beginning desorption of hot water temperature.The steam that desorption produces and air enter condenser 8, condenser coil 9 surface temperature is lower than dew-point temperature corresponding under this pressure, steam changes aqueous water into separates out on its surface, and wandered by Action of Gravity Field and collect in water-supporting disc 10 that condenser coil lower end is provided with, drain into fresh-water tank 12 by drain valve v-3.
When the first adsorbent bed 17 I adsorbance is tending towards saturated, at the end of the second adsorbent bed 17 II desorption, close weak solution pump b-1, cooling water pump b-3, heat-exchanger pump b-5, cooling tower 11, shutoff valve v-8, v-14, v-15, v-7, v-13, v-18.ON cycle fluid pump b-4, when the first adsorbent bed 17 I and the second adsorbent bed 17 II is cold and hot reach unanimity time, close circulation of fluid pump b-4, open valve v-10, v-9, v-6, v-16, v-12, v-17, open weak solution pump b-1, cooling water pump b-3, heat-exchanger pump b-5, cooling tower 11.
The now first end that partly circulates, rear half cycles starts, and correspondence system state point is B, and the first adsorbent bed 17 I starts desorption, and the second adsorbent bed 17 II starts absorption.
When the first adsorbent bed 17 I desorption terminates, when the second adsorbent bed 17 II absorption is tending towards saturated, close weak solution pump b-1, cooling water pump b-3, heat-exchanger pump b-5, cooling tower 11, shutoff valve v-10, v-9, v-17, v-12, v-6, v-16.ON cycle fluid pump b-4, when the first adsorbent bed 17 I and the second adsorbent bed 17 II is cold and hot reach unanimity time, close circulation of fluid pump b-4, open valve v-8, v-14, v-13, v-18, v-7, v-15, open weak solution pump b-1, cooling water pump b-3, heat-exchanger pump b-5, cooling tower 11.
Now system comes back to state point A, completes a circulation.Implement above-mentioned steps successively, make system between state point A and B, change i.e. the first adsorbent bed 17 I and the second adsorbent bed 17 II alternating sorbent desorption, the system that just can realize is run continuously.
The shutdown stage: close weak solution pump b-1, heat-exchanger pump b-5, cooling water pump b-3, cooling tower 11 successively, then guarantee that valve v-7, v-6, v-15, v-16, v-12, v-13, v-17, v-18 close, then guarantee that valve v-8, v-9, v-10, v-14 close.Finally close drain valve v-1, v-3.
By water-level gauge monitoring concentrated solution case 3 and fresh-water tank 12 water level, need when water level is too high to discharge liquid.Now for fresh-water tank 12, illustrate and how to take fresh water, concentrated solution is identical with it.After drain valve v-3 closes, valve v-4 opens automatically, and make pressure in fresh-water tank 12 return to normal pressure by vacuum, valve v-5 opens again, fresh water can flow out, drain rear valve v-5 to close, the vavuum pump be connected with valve v-4 is automatically opened and is extracted gas in casing, until with in vacuum chamber during pressure balance, the electromagnetism drain valve v-3 of both connections reopens, fresh water in dehydration plate 10 reenters fresh-water tank 12, carries out and so forth, realizes producing water continuously.
Inevitably there is the moisture of minute quantity in the air being inhaled into vavuum pump b-2, before air enters vavuum pump b-2 in this section, be provided with drier 7, effectively can absorb the moisture that this part is residual, ensure that entering the whole of vavuum pump b-2 is dry air, preventing from causing the lubricating condition deterioration of vavuum pump b-2 and the cavitation erosion of blade because absorbing steam, reduction of service life, making vavuum pump safe operation.
Vacuum atomizing flash distillation water separation device for salting liquid provided by the invention, for moisture in rapidly and efficiently separated salt solution, overcome existing technical disadvantages, by heat pipe intensified heat transfer, solid absorption drive, these three kinds of combine with technique of vacuum atomizing flash distillation, have capacity usage ratio high, less demanding to raw water quality, to advantages such as driving heat source temperature requirement are low, easy to control.
Although content of the present invention has done detailed introduction by above preferred embodiment, will be appreciated that above-mentioned description should not be considered to limitation of the present invention.After those skilled in the art have read foregoing, for multiple amendment of the present invention and substitute will be all apparent.Therefore, protection scope of the present invention should be limited to the appended claims.
Claims (9)
1. for a vacuum atomizing flash distillation water separation device for salting liquid, it is characterized in that, this device comprises evaporimeter (16), adsorbent bed (17), condenser (8), hot-water heating system and cooling water system;
Described hot-water heating system comprises the boiler (15) and heat exchanger (14) that are connected by pipeline;
Described cooling water system comprises the cooling water tank (13) and cooling tower (11) that are connected by pipeline;
Described evaporimeter (16) inside is provided with dividing plate (2), and is divided into closed two sections by described dividing plate (2), and epimere is vacuum chamber (5), and hypomere is hot hydroecium (1); Described evaporimeter (16) inside is also vertically provided with heat pipe group (4), and described heat pipe group (4) is through dividing plate (2), and the condensation segment of heat pipe group (4) and evaporator section lay respectively in described vacuum chamber (5) and hot hydroecium (1);
Described hot hydroecium (1) below is provided with pipeline and is connected with boiler (15) and heat exchanger (14) respectively; Described vacuum chamber (5) top is provided with pipeline and is connected with adsorbent bed (17); Described adsorbent bed (17) is also connected with condenser (8), cooling tower (11), heat exchanger (14), boiler (15) and cooling water tank (13) respectively by pipeline; Described condenser (8) is also connected with cooling tower (11) and cooling water tank (13) respectively by pipeline;
Pipeline between described boiler (15) and hot hydroecium (1) and adsorbent bed (17) is provided with heat-exchanger pump (b-5), hot water in boiler (15) can be pumped, then hot hydroecium (1) and adsorbent bed (17) is flowed through respectively, after described heat exchanger (14) heating, get back to described boiler (15) again, complete circulation;
Pipeline between described cooling water tank (13) and condenser and adsorbent bed (17) is provided with cooling water pump (b-3), cold water in cooling water tank (13) can be pumped, then condenser (8) and adsorbent bed (17) is flowed through respectively, after cooling tower (11) cooling, get back to described cooling water tank (13) again, complete circulation;
Described adsorbent bed (17) inside is also provided with can the solid absorbent of adsorb water vapor, and its adsorption pressure can reach 1kPa ~ 2kPa;
The heat pipe for thermal conductivity coefficient of described heat pipe group (4) is 10
5the W/ms order of magnitude;
The driving heat source that described device adopts comes from the low-grade heat source of 55-90 DEG C.
2., as claimed in claim 1 for the vacuum atomizing flash distillation water separation device of salting liquid, it is characterized in that, described vacuum chamber (5) inner upper is provided with atomization sprayer (6); Described atomization sprayer (6) is connected by the weak solution pump (b-1) that pipeline is outside with being arranged on evaporimeter (16); Described vacuum chamber (5) top is also provided with an entrance, and be provided with successively on the pipeline outside from this porch vacuum valve (v-2), drier (7) and and vavuum pump (b-2); Described vacuum chamber (5) bottom is provided with outlet, is connected with concentrated solution case (3) from the pipeline that this exit is outside, is provided with the first drain valve (v-1) between described concentrated solution case (3) and this outlet.
3. as claimed in claim 1 for the vacuum atomizing flash distillation water separation device of salting liquid, it is characterized in that, the pipeline that described vacuum chamber (5) top is connected with adsorbent bed (17) is provided with valve.
4. as claimed in claim 3 for the vacuum atomizing flash distillation water separation device of salting liquid, it is characterized in that, the pipeline between described adsorbent bed (17) and boiler (15) and cooling water tank (13) is respectively equipped with valve; Described adsorbent bed (17) and the pipeline between condenser (8), cooling tower (11) and heat exchanger (14) are also respectively equipped with valve.
5. as claimed in claim 4 for the vacuum atomizing flash distillation water separation device of salting liquid, it is characterized in that, described condenser (8) inside is provided with condenser coil (9), water-supporting disc (10) is provided with below it, be provided with at the bottom part down of this water-supporting disc (10) and lead to the outside opening of condenser (8), be connected with fresh-water tank (12) at this opening part by pipeline, the pipeline between this opening and fresh-water tank (12) is provided with the second drain valve (v-3).
6. as claimed in claim 4 for the vacuum atomizing flash distillation water separation device of salting liquid, it is characterized in that, it is one group that described adsorbent bed (17) adopts two, and often group comprises the first adsorbent bed (17 I) and the second adsorbent bed (17 II).
7. as claimed in claim 6 for the vacuum atomizing flash distillation water separation device of salting liquid, it is characterized in that, described the first adsorbent bed (17 I) and the second adsorbent bed (17 II) inside are respectively equipped with the first adsorbent bed internal duct (18) and the second adsorbent bed internal duct (19), and by its respectively all be connected cooling tower (11), heat exchanger (14), and cooling water tank (13), boiler (15) pipeline connection.
8. as claimed in claim 7 for the vacuum atomizing flash distillation water separation device of salting liquid, it is characterized in that, described heat exchanger (14) adopts shell-and-tube heat exchanger.
9. as claimed in claim 6 for the vacuum atomizing flash distillation water separation device of salting liquid, it is characterized in that, the pipeline between described the first adsorbent bed (17 I) and the second adsorbent bed (17 II) and boiler (15) and cooling water tank (13) is provided with circulation of fluid pump (b-4).
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| CN109915973A (en) * | 2019-03-29 | 2019-06-21 | 无锡商业职业技术学院 | A kind of air-conditioning refrigeration system of no refrigeration compressor |
| CN110508017A (en) * | 2019-08-14 | 2019-11-29 | 禹州市凯旋药业有限公司 | Liquid medicine concentration device is used in a kind of processing of Chinese medicine |
| CN111765550A (en) * | 2020-07-08 | 2020-10-13 | 南京工业大学 | Solution dehumidification and fresh water preparation composite system based on flash regeneration |
| CN113651384A (en) * | 2021-08-19 | 2021-11-16 | 东北电力大学 | Multistage injection flash evaporation seawater desalination system of coupling adsorption equipment |
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