CN104001342A - Vacuum atomizing flash evaporation water separation device for salt solution - Google Patents
Vacuum atomizing flash evaporation water separation device for salt solution Download PDFInfo
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- CN104001342A CN104001342A CN201410248369.4A CN201410248369A CN104001342A CN 104001342 A CN104001342 A CN 104001342A CN 201410248369 A CN201410248369 A CN 201410248369A CN 104001342 A CN104001342 A CN 104001342A
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Abstract
The invention discloses a vacuum atomizing flash evaporation water separation device for a salt solution. The separation device comprises an evaporator, an adsorption bed, a condenser, a hot water system and a cooling water system, wherein the hot water system comprises a hot water tank and a heat exchanger; the cooling water system comprises a cooling water tank and a cooling tower; a baffle is arranged in the evaporator; the upper section of the evaporator is a vacuum chamber; the lower section of the evaporator is a hot water chamber; a cluster of hot pipes, which penetrate through the baffle, are also arranged; the hot water chamber is connected with the hot water tank and the heat exchanger; the vacuum chamber is connected with the adsorption bed which is connected with the condenser, the cooling tower, the heat exchanger, the hot water tank and the cooling water tank; the condenser is connected with the cooling tower and the cooling water tank; hot water pumps are arranged on a pipeline between the hot water tank and the hot water chamber and a pipeline between the hot water tank and the adsorption bed; cooling water pumps are arranged on a pipeline between the cooling water tank and the condenser and a pipeline between the cooling water tank and the adsorption bed. The vacuum atomizing flash evaporation water separation device of the salt solution has the advantage of being high in energy utilization rate, low in raw water quality requirement and driving heating source temperature requirement and 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 salting liquid vacuum atomizing flash distillation water separation device that drives and utilize heat pipe intensified heat transfer based on solid absorption.
Background technology
In recent years, solution dehumidification technology has obtained development faster, and solution dehumidification system can adopt low-temperature heat source to drive, and utilizes the salting liquid that possesses strong wettability power to carry out caloic exchange with humid air in dehumidifier, and then reaches the object of air dewetting.It has overcome the problem of freeze drying consumption 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 version of solution dehumidification system is roughly divided into following several at present: interior pattern of fever regenerator, heat insulation-type regenerator, solar energy heating type regenerator, vaporation-type regenerator.
Wherein, interior pattern of fever regenerator compensates due to the heat that in solution, moisture evaporation is taken away by external heat source, and maintaining actified solution has certain temperature, is similar to isothermal regeneration, has guaranteed the pressure differential power of regenerative process, has improved regeneration efficiency.As shown in Figure 1.Weak solution is sent into successively and in preheater, heater, is carried out preheating by solution pump by bottom, improve solution water steam surface steam pressure, then spray on the packing layer of regenerator, contact with air, in solution, steam is exchanged and is pulled away by caloic, due to moisture evaporation endothermic, solution temperature reduces, and the solution circulation after cooling enters heater and heats.Although cyclic process has guaranteed 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 wider, itself is Shortcomings still, and as comparatively complicated in apparatus and process, regeneration efficiency is restricted etc.Therefore when 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, has obtained tremendous development in recent years at aspects such as membrane module performance, Energy Recovery Technologies, makes water cost to decline to a great extent, and it produces water capacity and has accounted for the more than 50% of desalinization total capacity.Thermal distillation method for desalting seawater is mainly used in the coproduction of electricity-water at present, 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 the low-grade heat sources such as industrial afterheat recovery and solar thermal energy, geothermal energy.
In the application of desalinization field for many years, Fig. 2 is its single-stage schematic diagram to multi-stage flash evaporation technology based on flash distillation theory.Upper level seawater enters this grade of flash distillation by throttle nozzle, and the moisture flashing off condenses by the condensation tube bank on top, and condensate liquid is collected and discharged by fresh water dish.
From above introduction, can see, solution dehumidification technology take that to improve cocnentration factor be goal in research, and multistage flash evaporation seawater desalting is that to improve water generation ratio be research direction, although both objects are different, but its core essence is in full accord, by heat-driven and vacuum degree control, the moisture in separation solution as far as possible fast and efficiently.And the initial flash temperature that the continuous separated fundamental driving force of moisture is solution and cooling water temperature is poor, under certain vacuum degree condition, the speed of the indirect condensate water steam of cooling water 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, approach 8～50kPa, reduced the degree of superheat of solution entrance, restricted evaporation ends evaporation efficiency; (2) because of the temperature reference of commonly using cooling water, (seawater desalination system cooling water mainly adopts seawater, general 25 ℃ of left and right, dehumidification solution regeneration adopts cooling tower cooling water, general 32 ℃ upper and lower), can utilize low-grade heat source range to be restricted, during such as 60 ℃ of solution multistage flash evaporations regeneration of employing, both temperature difference only have 28 ℃, progression can be set and be restricted.
With regard to solution flash process, there are 2 deficiencies: this is a face evaporation for (1), and disengagement area is limited; (2) along with continuing that moisture evaporates, main body solution temperature fast reducing, the degree of superheat reduces even to disappear, and its evaporation intensity also weakens thereupon.
Obviously, for the solution in evaporation process provides enough heats, become the key factor that keeps its evaporation intensity, the coagulability that condenser matches is simultaneously also that this process can continue the important step of carrying 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 multistage utilization based on heat, but therefore the limited caving-in bash of single-stage evaporation amount improves single-stage evaporation amount and heat utilization rate and can optimize whole system design.
Summary of the invention
The object of this invention is to provide a kind of for the device of separated salt solution moisture rapidly and efficiently, overcome existing technical disadvantages, by heat pipe intensified heat transfer, solid absorption drive, these three kinds of technology combinations 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 boiler and the heat exchanger connecting by pipeline; Described cooling water system comprises cooling water tank and the cooling tower connecting by pipeline; Described evaporimeter inside is provided with dividing plate, and by described dividing plate, is divided into the two sections of sealing, 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 heat pipe group's condensation segment and evaporator section lay respectively in described vacuum chamber and hot hydroecium; Described hot hydroecium below is provided with pipeline and is connected with boiler and heat exchanger respectively; Described vacuum chamber top is provided with pipeline and is 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 respectively hot hydroecium and adsorbent bed, 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, and then flow through respectively condenser and adsorbent bed, then after cooling tower is cooling, get back to described cooling water tank, complete circulation.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, described internal vacuum chamber top is provided with atomization sprayer; Described atomization sprayer is connected with the weak solution pump that is arranged on evaporimeter outside by pipeline; Described vacuum chamber side is also provided with an entrance, and on the pipeline outside from this porch, be provided with successively vacuum valve, drier and and vavuum pump; Drier can absorb residual water vapor, guarantees the normal safe operation of vavuum pump; Described vacuum chamber bottom is provided with outlet, from the outside pipeline in this exit, is connected with concentrated solution case, between described concentrated solution case and this outlet, is provided with the first drain valve.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, the pipeline that described vacuum chamber top is connected with adsorbent bed is provided with valve.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, is respectively equipped with valve on the pipeline between described adsorbent bed and boiler and cooling water tank; On pipeline between described adsorbent bed and condenser, cooling tower and heat exchanger, be 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, its below is provided with water-supporting disc, below the bottom of this water-supporting disc, be provided with the opening that leads to condenser outside, at this opening part, by pipeline, be connected with fresh-water tank, 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, it is one group that described adsorbent bed adopts two, every group comprises the first adsorbent bed and the second adsorbent bed, can increase group number according to steam flow.Two adsorbent beds are alternately connected with cold water or hot water, to realize adsorption and desorption simultaneously, guarantee 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 the pipeline connection of cooling water tank, boiler, making can to pass into cooling water in the first adsorbent bed internal duct and the second adsorbent bed internal duct keeps adsorption capacity to saturated, and circulate, the low-grade hot water that also can pass into 55-90 ℃ 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 solid absorbent that can adsorbed water steam, 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:
Vavuum pump b-2 vacuumizes final vacuum valve v-2 by system and closes; Salting liquid through low-grade heat source preheating is pumped to atomization sprayer, becomes fine droplets and sprayed to vacuum chamber flash distillation after atomization, is full of whole vacuum chamber; During flash distillation, atomized soln body temperature declines rapidly, but absorb rapidly heat on heat pipe group surface, elevates the temperature, and the degree of superheat increases, and forms double evaporation-cooling; Now hot intraductal working medium, at upper end condensation heat, is back to lower end under Action of Gravity Field, in hot hydroecium, absorbs heat and evaporation again, and salting liquid, because moisture flash distillation becomes concentrated solution, is collected into concentrated solution case by drain valve v-1 after vacuum chamber bottom is gathered; When flash distillation starts, vacuum indoor pressure, because moisture evaporation sharply increases, utilizes solid absorbent steam to strong adsorption effect, such as silica gel, zeolite etc., its adsorption pressure can reach 1kPa～2kPa, and Quick Catch steam, to maintain vacuum; When steam is adsorbed, can emit a large amount of heats of adsorption, by keeping adsorption capacity to the logical cooling water of adsorbent bed; When absorption is tending towards saturated, to adsorbent bed, pass to the low-grade hot water of 55-90 ℃, solid absorbent is carried out to desorption; The steam producing during desorption, at condenser coil surface condensation, becomes water droplet, drips and accumulates on water-supporting disc, finally flows in fresh-water tank; By valve, switch, make adsorbent bed replace adsorption/desorption, can guarantee water separation process continue carry out.Wherein cooling water and hot water are provided by the cooling water system hot-water heating system of unifying, and form the interior circulation of sealing.
The above-mentioned vacuum atomizing flash distillation water separation device for salting liquid, wherein, described heat pipe group's heat pipe for thermal conductivity coefficient 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 ℃, 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 can be isolated moisture fast by the method for vacuum flashing, becomes concentrated solution and fresh water.
2. atomization makes solution become fine droplets, can not only greatly increase flash separation face, and can obviously lengthen the suspension time of drop, is 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 because of flash distillation fast cooling, keep even improving the degree of superheat of drop, on the heat pipe surface of isothermal, form secondary heat absorption evaporation, there is higher evaporation rate.
4. by changing topping up working medium and liquid filled ratio, the mode such as be evacuated, can mate the low-temperature heat source under different temperatures.
5. driving heat source comes from the low-grade heat source of 55-90 ℃, 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, has higher evaporation rate.
7. suitably regulate salting liquid temperature and the cold water temperature difference can control and regulate vacuum pressure, guarantee flash process continue carry out, vavuum pump only uses when manufacturing initial vacuum and getting rid of incoagulable gas.
8. the many adsorbent beds of employing switch, and take backheat measure, continuation and the raising thermal efficiency of the operation of energy assurance system.
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 processing waste water, sewage etc., 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 that the present invention is for the structural representation of the vacuum atomizing flash distillation water separation device of salting liquid.
Fig. 4 is that the present invention is for the adsorbent bed partial schematic diagram of the vacuum atomizing flash distillation water separation device of salting liquid.
The specific embodiment
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 boiler 15 and the heat exchanger 14 connecting by pipeline.Heat exchanger 14 adopts shell-and-tube heat exchanger.
Cooling water system comprises cooling water tank 13 and the cooling tower 11 connecting by pipeline.
Evaporimeter 16 inside are provided with dividing plate 2, and by dividing plate 2, are divided into the two sections of sealing, and epimere is vacuum chamber 5, and hypomere is hot hydroecium 1; Evaporimeter 16 inside are also vertically provided with heat pipe group 4, and heat pipe group 4 is through dividing plate 2, and heat pipe group 4 condensation segment and evaporator section lay respectively in vacuum chamber 5 and hot hydroecium 1.
Vacuum chamber 5 inner and upper are provided with atomization sprayer 6; Atomization sprayer 6 is connected with the weak solution pump b-1 that is arranged on evaporimeter 16 outsides by pipeline; Vacuum chamber 5 tops are also provided with an entrance, and on the pipeline outside from this porch, be provided with successively vacuum valve v-2, drier 7 and and vavuum pump b-2; Drier 7 can absorb residual water vapor, guarantees normal, the safe operation of vavuum pump b-2, by vavuum pump b-2, can connect external device (ED); Vacuum chamber 5 bottoms are provided with outlet, from the outside pipeline in this exit, are connected with concentrated solution case 3, are provided with the first drain valve v-1 between concentrated solution case 3 and this outlet.
Hot hydroecium 1 below is provided with pipeline and is connected with boiler 15 and heat exchanger 14 respectively; Vacuum chamber 5 tops are provided with pipeline and are connected with adsorbent bed 17.The pipeline that vacuum chamber 5 tops are connected with adsorbent bed 17 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 are provided with solid absorbent that can adsorbed water steam, and such as silica gel, zeolite etc., its adsorption pressure can reach 1kPa～2kPa.It is one group that adsorbent bed 17 adopts two, and every group comprises the first adsorbent bed 17 I and the second adsorbent bed 17 II, can increase group number according to steam flow, and two adsorbent beds 17 are alternately connected with cold water or hot water, to realize adsorption and desorption simultaneously, guarantee carrying out continuously of process.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 the pipeline connection of cooling water tank 13, boiler 15, making can to pass into cooling water in the first adsorbent bed internal duct 18 and the second adsorbent bed internal duct 19 keeps adsorption capacity to saturated, and circulate, the low-grade hot water that also can pass into 55-90 ℃ 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.Between two transfer periods, the hot and cold water blending of adsorbent bed 17 internal duct is flowed, and realizes the backheat between two.On pipeline between adsorbent bed 17 and boiler 15 and cooling water tank 13, be respectively equipped with valve v-16, v-18 and v-15, v-17; On pipeline between adsorbent bed 17 and condenser 8, cooling tower 11 and heat exchanger 14, be 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 are provided with condenser coil 9, its below is provided with water-supporting disc 10, below the bottom of this water-supporting disc 10, be provided with the opening that leads to condenser 8 outsides, at this opening part, by pipeline, be connected with fresh-water tank 12, the pipeline between this opening and fresh-water tank 12 is provided with the second drain valve v-3.On fresh-water tank 12, be also provided with valve v-4 and v-5.Drain valve v-1 and v-3 are normally open valve, by the power supply of vavuum pump b-2, control, and vavuum pump b-2 closes while opening, and vavuum pump b-2 opens draining while quitting work.
Pipeline between boiler 15He 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 respectively hot hydroecium 1 and adsorbent bed 17, 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 respectively condenser 8 and adsorbent bed 17, then after cooling tower 11 is cooling, get back to cooling water tank 13, 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 ℃, comprises solar energy and industrial exhaust heat, used heat etc.First, vavuum pump b-2 vacuumizes final vacuum valve v-2 by system and closes; Salting liquid through low-grade heat source preheating is pumped to atomization sprayer 6, becomes fine droplets and sprayed to vacuum chamber 5 flash distillations after atomization, is full of whole vacuum chamber 5; During flash distillation, atomized soln body temperature declines rapidly, but absorb rapidly heat on heat pipe group 4 surfaces, elevates the temperature, and the degree of superheat increases, and forms double evaporation-cooling; Heat pipe group 4 heat pipe for thermal conductivity coefficient is 10
5the W/ms order of magnitude; Now hot intraductal working medium is at upper end condensation heat, under Action of Gravity Field, be back to lower end, in hot hydroecium 1, absorb heat and evaporation again, salting liquid, because moisture flash distillation becomes concentrated solution, is collected into concentrated solution case 3 by drain valve v-1 after vacuum chamber 5 bottoms are gathered; When flash distillation starts, vacuum chamber 5 internal pressures, because of sharply increase of moisture evaporation, are utilized solid absorbent steam to strong adsorption effect, such as silica gel, zeolite etc., its adsorption pressure can reach 1kPa～2kPa, and Quick Catch steam, to maintain vacuum; When steam is adsorbed, can emit a large amount of heats of adsorption, by keeping adsorption capacity to the logical cooling water of adsorbent bed 17; When absorption is tending towards saturated, pass to the low-grade hot water of 55-90 ℃ to adsorbent bed 17, solid absorbent is carried out to desorption; The steam producing during desorption, at condenser coil 9 surface condensations, becomes water droplet, drips and accumulates on water-supporting disc 10, finally flows in fresh-water tank 12; By valve, switch, make the first adsorbent bed 17 I and the second adsorbent bed 17 II replace adsorption/desorption, can guarantee water separation process continue carry out.Wherein cooling water and hot water are provided by the cooling water system hot-water heating system of unifying, and form the interior circulation of sealing.
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, and starting power supply is 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, make the first adsorbent bed 17 I and the second adsorbent bed 17 II all in cryogenic absorption state, and heat pipe group 4 is heated up, internal working medium is subject to thermal evaporation; Vavuum pump b-2 starts, and now vacuum valve v-2, v-8, v-9, v-10, v-14 open, and valve v-4, v-5 close.
By pressure gauge, observing vacuum chamber 5 internal pressures changes, vavuum pump b-2 is pumped to while approaching limiting condition, close vavuum pump b-2 and vacuum valve v-2, v-8, v-9, v-14, open weak solution pump b-1, extraction is through the weak solution of preheating, and be pressed into the atomization sprayer 6 that is contained in vacuum chamber 5 middle and upper parts, weak solution atomization in atomization sprayer 6, spray is to the interior flash distillation of vacuum chamber 5, during flash distillation, atomized soln body temperature declines rapidly, but absorb rapidly heat on heat pipe group 4 heat pipe surface, elevate the temperature, the degree of superheat increases, and forms double evaporation-cooling.Now hot intraductal working medium, at upper end condensation heat, is back to lower end under Action of Gravity Field, in hot hydroecium 1, absorbs heat and evaporation again.The steam flashing off is adsorbed to maintain the vacuum of flash process under the second adsorbent bed 17 II absorption affinities drive, and the concentrated solution after flash distillation is gathered in vacuum chamber 5 bottoms, by drain valve v-1, drains into concentrated solution case 3.
By pressure gauge, observe, when the second adsorbent bed 17 II adsorbances are tending towards saturated, shut off 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 starting stage of starting shooting finishes, and first half circulation of operation circulation starts continuously, is now system mode point A.The first adsorbent bed 17 I start the steam that absorption flashes off, and the second adsorbent bed 17 II pass into the upper high desorption that starts of hot water temperature.Steam and air that desorption produces enter condenser 8, condenser coil 9 surface temperatures are lower than dew-point temperature corresponding under this pressure, steam changes aqueous water into separates out on its surface, and wander and collect in the water-supporting disc 10 that condenser coil lower end is provided with by Action of Gravity Field, by drain valve v-3, drain into fresh-water tank 12.
When the first adsorbent bed 17 I adsorbances are tending towards saturated, when the second adsorbent bed 17 II desorptions finish, close weak solution pump b-1, cooling water pump b-3, heat-exchanger pump b-5, cooling tower 11, shut off 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 cold and hot the reaching unanimity of the second adsorbent bed 17 II, 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.
Now first half circulation finishes, and rear half cycles starts, and correspondence system state point is B, and the first adsorbent bed 17 I start desorption, and the second adsorbent bed 17 II start absorption.
When the first adsorbent bed 17 I desorptions finish, when the second adsorbent bed 17 II absorption are tending towards saturated, close weak solution pump b-1, cooling water pump b-3, heat-exchanger pump b-5, cooling tower 11, shut off 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 cold and hot the reaching unanimity of the second adsorbent bed 17 II, 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, has completed a circulation.Implement successively above-mentioned steps, it is that the first adsorbent bed 17 I and the second adsorbent bed 17 II replace adsorption/desorption that system is changed between state point A and B, and the system that just can realize is moved continuously.
The shutdown stage: close successively weak solution pump b-1, heat-exchanger pump b-5, cooling water pump b-3, cooling tower 11, 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, monitor concentrated solution case 3 and fresh-water tank 12 water levels, when water level is too high, need to discharge liquid.Now take fresh-water tank 12 as example, illustrate how to take fresh water, concentrated solution is identical with it.After drain valve v-3 closes, valve v-4 opens automatically, makes fresh-water tank 12 internal pressures return to normal pressure by vacuum, and valve v-5 opens again, fresh water can flow out, drain rear valve v-5 and close, the vavuum pump being connected with valve v-4 is automatically opened and is extracted gas in casing, until during with vacuum chamber internal pressure balance, the electromagnetism drain valve v-3 that connects both reopens, fresh water in dehydration plate 10 reenters fresh-water tank 12, carries out and so forth, realizes and produces continuously water.
Inevitably can there is the moisture of minute quantity in the air that is inhaled into vavuum pump b-2, before air enters vavuum pump b-2 in this section, be provided with drier 7, can effectively absorb this part residual moisture, it is dry air that assurance enters the whole of vavuum pump b-2, prevent from causing the lubricating condition deterioration of vavuum pump b-2 and the cavitation erosion of blade because absorbing steam, reduction of service life, make vavuum pump safe operation.
Vacuum atomizing flash distillation water separation device for salting liquid provided by the invention, be used for rapidly and efficiently separated salt solution moisture, overcome existing technical disadvantages, by heat pipe intensified heat transfer, solid absorption drive, these three kinds of technology combinations 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 been done detailed introduction by above preferred embodiment, will be appreciated that above-mentioned description should not be considered to limitation of the present invention.Those skilled in the art, read after foregoing, for multiple modification of the present invention with to substitute will be all apparent.Therefore, protection scope of the present invention should be limited to the appended claims.
Claims (10)
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 boiler (15) and the heat exchanger (14) connecting by pipeline;
Described cooling water system comprises cooling water tank (13) and the cooling tower (11) connecting by pipeline;
Described evaporimeter (16) inside is provided with dividing plate (2), and by described dividing plate (2), is divided into the two sections of sealing, 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 heat pipe group's (4) condensation segment 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 flow through respectively hot hydroecium (1) and adsorbent bed (17), 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 flow through respectively condenser (8) and adsorbent bed (17), after cooling tower (11) is cooling, get back to again described cooling water tank (13), complete circulation.
2. the vacuum atomizing flash distillation water separation device for salting liquid as claimed in claim 1, is characterized in that, described vacuum chamber (5) inner and upper is provided with atomization sprayer (6); Described atomization sprayer (6) is connected by the pipeline weak solution pump (b-1) outside with being arranged on evaporimeter (16); Described vacuum chamber (5) top is also provided with an entrance, and on the pipeline outside from this porch, be provided with successively vacuum valve (v-2), drier (7) and and vavuum pump (b-2); Described vacuum chamber (5) bottom is provided with outlet, from the outside pipeline in this exit, is connected with concentrated solution case (3), between described concentrated solution case (3) and this outlet, is provided with the first drain valve (v-1).
3. the vacuum atomizing flash distillation water separation device for salting liquid as claimed in claim 1, is characterized in that, the pipeline that described vacuum chamber (5) top is connected with adsorbent bed (17) is provided with valve.
4. the vacuum atomizing flash distillation water separation device for salting liquid as claimed in claim 3, is characterized in that, on the pipeline between described adsorbent bed (17) and boiler (15) and cooling water tank (13), is respectively equipped with valve; On pipeline between described adsorbent bed (17) and condenser (8), cooling tower (11) and heat exchanger (14), be also respectively equipped with valve.
5. the vacuum atomizing flash distillation water separation device for salting liquid as claimed in claim 4, it is characterized in that, described condenser (8) inside is provided with condenser coil (9), its below is provided with water-supporting disc (10), in the below, bottom of this water-supporting disc (10), be provided with and lead to the outside opening of condenser (8), at this opening part, by pipeline, be connected with fresh-water tank (12), the pipeline between this opening and fresh-water tank (12) is provided with the second drain valve (v-3).
6. the vacuum atomizing flash distillation water separation device for salting liquid as claimed in claim 4, is characterized in that, it is one group that described adsorbent bed (17) adopts two, and every group comprises the first adsorbent bed (17 I) and the second adsorbent bed (17 II).
7. the vacuum atomizing flash distillation water separation device for salting liquid as claimed in claim 6, it is characterized in that, the first described 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 the pipeline connection of cooling water tank (13), boiler (15).
8. the vacuum atomizing flash distillation water separation device for salting liquid as claimed in claim 7, is characterized in that, described heat exchanger (14) adopts shell-and-tube heat exchanger.
9. the vacuum atomizing flash distillation water separation device for salting liquid as claimed in claim 6, it is characterized in that, the pipeline between the first described 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).
10. the vacuum atomizing flash distillation water separation device for salting liquid as claimed in claim 6, is characterized in that, described adsorbent bed (17) is inner be also provided with can adsorbed water steam solid absorbent, its adsorption pressure can reach 1kPa～2kPa.
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| CN104001342B (en) | 2015-12-30 |
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