CN204815761U - Crystallization liquid desalination equipment - Google Patents
Crystallization liquid desalination equipment Download PDFInfo
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- CN204815761U CN204815761U CN201520413567.1U CN201520413567U CN204815761U CN 204815761 U CN204815761 U CN 204815761U CN 201520413567 U CN201520413567 U CN 201520413567U CN 204815761 U CN204815761 U CN 204815761U
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- crystal solution
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
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- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The utility model relates to a crystallization liquid desalination equipment, equipment includes exclusive use or the demineralization accumulator still that establish ties to use and removes the salt oven, removes the crystallization liquid entry of salt oven and is connected with the bin outlet of evaporation crystallization kettle through crystallization liquid discharging pump and pipeline, or the crystallization liquid exit linkage through crystallization liquid discharging pump and pipeline and demineralization accumulator still. The stifled pipe problem of scale deposit outside the multiple effect evaporation system has effectively been solved to this equipment, has still solved the contradiction problem of crystallization liquid concentration with the velocity of flow, how does not have wheel crystallization liquid flow velocity, and the heat that saturated salt solution was taken is retrieved to the homoenergetic, falls end steam consumption.
Description
Technical field
The utility model relates to crystallization technical field of auxiliary equipment, is specifically related to a kind of crystal solution demineralization plant.
Background technology
Multiple-effect evaporation (referring generally to triple effect) concentration technique has been widely applied to the industry such as chemical industry, pharmacy as energy saving technology, particularly in process high-salt wastewater, shows great advantage.
Chinese patent document CN201168457Y discloses a kind of Multi-effect evaporation crystallizer, and this system is made up of an effect heater and 1st effective evaporator, two effect heaters and 2nd effect evaporator, triple effect heater and triple effect evaporation crystallizer and steam-water separator, cooler, drop pan, vavuum pump.It is characterized in that being provided with forced circulation pump between heater and evaporimeter, below 1st effective evaporator, 2nd effect evaporator and triple effect evaporation crystallizer, be respectively provided with a crystallization leg.This is the typical process (in the multiple-effect evaporation technique had, flow direction of material unlike this) of current multiple-effect evaporation concentration technique, effectively can solve Multi-effect evaporation crystallizer intrasystem fouling plugging problem.But outside system, no longer include heating facility from crystal solution discharging pump to crystallization tank, be a process of lowering the temperature gradually, therefore this section is also the district occurred frequently of fouling plugging.Because in above-mentioned technique, crystal solution discharging pump is continuous operation, therefore there is such conflict, when crystal solution discharge is less, discharging pump flow is little, and flow velocity is slow, in pump or after pump, easily fouling and clogging occurs; When crystal solution load is larger, crystal solution concentration is lower, take a large amount of high temperature saturated brines out of, after crystallization tank cooling, return multi-effect evaporation system, cause energy waste, make whole multi-effect evaporation system work efficiency drop, in addition, after a large amount of saturated brine mixes with the fresh less salt waste water in cistern, salt content is improved, adds the possibility of multi-effect evaporation system intercrystalline plugging.
Utility model content
The purpose of this utility model is to overcome defect of the prior art, designs a kind of not only energy-conservation but also can prevent the crystal solution demineralization plant of crystal solution fouling plugging.
For achieving the above object, the technical scheme that the utility model adopts is:
A kind of crystal solution demineralization plant, it is characterized in that, described equipment comprises the desalination accumulator still of the use that is used alone or connects and removes salt oven, described desalination accumulator still comprises kettle, reductor, sealed stirrer, crystal solution entrance, crystal solution outlet and concentration analyzer, crystal solution entrance is positioned at kettle top, concentration analyzer is positioned at still near kettle top, and crystal solution outlet is positioned at the bottom of kettle, and crystal solution entrance is connected by pipeline with the discharge gate of evaporative crystallization still; Except salt oven comprises crystal solution entrance, saturated brine refluxing opening, crystal salt outlet, drain and concentration analyzer, the still top that saturated brine refluxing opening except salt oven is positioned at except salt oven is in cap shape structure, except the crystal solution entrance of salt oven is positioned at kettle upper portion side wall, except the drain of salt oven is near autoclave body bottom, except the concentration analyzer in salt oven is near kettle top, except the crystal salt outlet of salt oven is near autoclave body bottom; Except the crystal solution entrance of salt oven is connected with the discharge gate of evaporative crystallization still by crystal solution discharging pump and pipeline, or pass through crystal solution discharging pump and pipeline and export with the crystal solution of desalination accumulator still and be connected.
Wherein preferred technical scheme is that the diameter that the described crystal salt except salt oven exports is greater than 400mm.
Preferred technical scheme also has, and described desalination accumulator still is respectively equipped with the outside except salt oven the concentration display be connected with concentration analyzer.
Preferred technical scheme also has, and discharge gate and the vertical direction angle of described evaporative crystallization still are not more than 135 °.
Preferred technical scheme also has, and be provided with chuck at the outer wall of described evaporative crystallization still, chuck is provided with water inlet and delivery port, and water inlet is connected with heater by water pipe and water pump with delivery port.
Advantage of the present utility model is with beneficial effect: described crystal solution demineralization plant prior art is compared, efficiently solve the fouling plugging problem outside multi-effect evaporation system, also solve the contradictory problems of crystal solution concentration and flow velocity, how do not take turns the crystal solution rate of outflow, equal can reclaim saturated brine with heat, end steam consumption falls.
Accompanying drawing explanation
Fig. 1 is the structural representation of desalination accumulator still in the utility model crystal solution demineralization plant;
Fig. 2 is the structural representation that in the utility model crystal solution demineralization plant, desalination is slow;
Fig. 3 is the structural representation of embodiment 1 in the utility model crystal solution demineralization plant;
Fig. 4 is the structural representation of embodiment 2 in the utility model crystal solution demineralization plant;
Fig. 5 is the structural representation of embodiment 3 in the utility model crystal solution demineralization plant.
In figure: 1, crystal solution entrance; 2, desalination accumulator still; 3, concentration analyzer; 4, agitator; 5, crystal solution outlet; 6, reductor; 7, concentration display;
11, crystal solution entrance; 12, saturated brine refluxing opening; 13, concentration analyzer; 14 crystal salt outlets; 15, drain; 16, except salt oven; 17, concentration display;
20, heater; 21, evaporative crystallization still; 22, forced circulation pump; 23, crystal solution discharging pump; 24, the vertical angle between desalination accumulator still and evaporative crystallization still.
Detailed description of the invention
Below in conjunction with drawings and Examples, detailed description of the invention of the present utility model is further described.Following examples only for clearly the technical solution of the utility model being described, and can not limit protection domain of the present utility model with this.
As shown in Figure 1: desalination accumulator still comprises crystal solution entrance 1, desalination accumulator still 2, concentration analyzer 3, agitator 4, crystal solution outlet 5, reductor 6 and concentration display 7.
As shown in Figure 2: except salt oven comprise crystal solution entrance 11, saturated brine refluxing opening 12, concentration analyzer 13, crystal salt outlet 14, drain 15, except salt oven 16 and concentration display 17.
Embodiment 1
As shown in Figure 3, be arranged on by desalination accumulator still 2 below evaporative crystallization still 21, discharge nozzle and the vertical direction angle 24 of evaporative crystallization still are not more than 135 °.High dense crystal solution directly flows to desalination accumulator still 2 by evaporative crystallization still 21 and keeps in, and flow passes through valve regulated.The concentration of still intercrystalline salt is obtained by the display of concentration analyzer 3 and concentration display 7, when dense crystal solution high in desalination accumulator still 2 be accumulated to a certain amount of after, open reductor 6, agitator 4 pairs of crystal solution are driven to stir, the crystal salt of partly sedimentation is mixed with top saturated brine, then crystal solution discharging pump 23 is opened, dense for height in desalination accumulator still 2 crystal solution is once pumped, the interior cooling of the groove that decrystallizes, crystallization desalination, drench the saturated brine, again enter crystal solution demineralization plant and process.
Embodiment 2
As shown in Figure 4, by crystal solution discharging pump 23, crystal solution is pumped into except in salt oven 16 from crystal solution entrance 11.Be pumped to saturated brine in the crystal solution promotion still except salt oven 16 to move to still cap shape structure, and then saturated brine is flowed out by saturated brine refluxing opening 11 again enter evaporative crystallization still 21, heater 20 circulatory system, supplement the water level of crystal solution demineralization plant in time, do not affect the upper doses of the former water of saliferous.Meanwhile, be pumped to except the crystal solution of salt oven 16 is in movement forward, achieve sedimentation separation, crystal salt is sunk at the bottom of still, and saturated brine moves to still top.Obtained the concentration of still intercrystalline salt by the display of concentration analyzer 13 and concentration display 17, when still intercrystalline mineralization is to after a certain amount of, stop to this except salt oven 16 pumps into crystal solution.Open drain 11 valve, make the saturated brine of still internal upper part remnants drench.Afterwards, open out crystal salt outlet 14, salt is dug out pack.
Embodiment 3
As shown in Figure 5, desalination accumulator still 2 is arranged on below evaporative crystallization still 21, and discharge nozzle and the lower vertical direction angle 24 of evaporative crystallization still are not more than 135 °.High dense crystal solution directly flows to desalination accumulator still 2 by evaporative crystallization still 21 and keeps in, and flow passes through valve regulated.Pass through.The concentration of still intercrystalline salt is obtained by the display of concentration analyzer 3 and concentration display 7, when dense crystal solution high in desalination accumulator still 2 be accumulated to a certain amount of after, open reductor 6, stirring 4 pairs of crystal solution are driven to stir, the crystal salt of partly sedimentation is mixed with top saturated brine, then crystal solution discharging pump 23 is opened, dense for height in desalination accumulator still 2 crystal solution is once pumped into desalination still 16, the dense crystal solution of height newly entered except salt oven 16 impels still internal upper part saturated brine to get back to multi-effect evaporation system by the structural saturated brine return pipe 11 of still cap shape, self be also able to sedimentation separation simultaneously, salt sinks at the bottom of still.Pass through.Obtained the concentration of still intercrystalline salt by the display of concentration analyzer 13 and concentration display 17, when mineralization is to after a certain amount of, stop to this except salt oven 16 pumps into crystal solution.Open discharging valve door, make the saturated brine of still internal upper part remnants drench.Afterwards, open salt-overflowing hole, salt is dug out pack.
Evaporative crystallization still, desalination accumulator still are connected successively with crystal solution discharging pump in embodiment 1.Desalination accumulator still is arranged on below evaporative crystallization still, and discharge nozzle and the vertical direction angle of evaporative crystallization still are not more than 135 °.High dense crystal solution relies on potential difference, flows into desalination accumulator still, by the rate of outflow of Valve controlling crystal solution under gravity by evaporative crystallization still.By concentration analyzer and concentration display, when accumulator still intercrystalline liquid be accumulated to a certain amount of after, turn on agitator, the salt of the sedimentation of part in still is mixed with the saturated brine on upper strata, then opens discharging pump, dense for the height in accumulator still crystal solution is once pumped, the interior cooling of the groove that decrystallizes, crystallization desalination, drenches the saturated brine, and again enters multi-effect evaporation system and processes.
Evaporative crystallization still, crystal solution discharging pump are connected successively with except salt oven in example 2.Crystal solution pumps from steaming in crystallization kettle with comparatively large discharge by crystal solution discharging pump, pumps into from the crystal solution entrance except salt oven.Be pumped to saturated brine in the crystal solution promotion still except salt oven to move to still cap shape structure, and then make saturated brine again enter evaporative crystallization still, the heating kettle circulatory system by the outflow of saturated brine refluxing opening, supplement the water level of multiple-effect evaporation still system in time, do not affect the upper doses of the former water of saliferous.Meanwhile, be pumped to except the crystal solution of salt oven is in movement forward, achieve sedimentation separation, crystal salt is sunk at the bottom of still, and saturated brine moves to still top.By concentration analyzer and concentration display, when still intercrystalline mineralization is to after a certain amount of, stop to this except salt oven pumps into crystal solution.Open discharging valve door, make the saturated brine of still internal upper part remnants drench.Afterwards, open crystal salt outlet, salt is dug out pack.
Evaporative crystallization still, desalination accumulator still, crystal solution discharging pump are connected successively with except salt oven in embodiment 3.Desalination accumulator still is arranged on below evaporative crystallization still, and discharge nozzle and the lower vertical direction angle of evaporative crystallization still are not more than 135 °.High dense crystal solution relies on potential difference, flows into desalination accumulator still, by the rate of outflow of Valve controlling crystal solution under gravity by evaporative crystallization still.By concentration analyzer and concentration display, when accumulator still intercrystalline liquid be accumulated to a certain amount of after, turn on agitator, the salt of the sedimentation of part in still is mixed with the saturated brine on upper strata, then discharging pump is opened, dense for height in accumulator still crystal solution is once pumped into desalination still, be pumped to saturated brine in the crystal solution promotion still except salt oven to move to still cap shape structure, and then make saturated brine again enter evaporative crystallization still, the heating kettle circulatory system by the outflow of saturated brine refluxing opening, reduce energy loss.Meanwhile, be pumped to except the crystal solution of salt oven is in movement forward, achieve sedimentation separation, crystal salt is sunk at the bottom of still, and saturated brine moves to still top.By concentration analyzer and concentration display, when still intercrystalline mineralization is to after a certain amount of, stop to this except salt oven pumps into crystal solution.Open discharging valve door, make the saturated brine of still internal upper part remnants drench.Afterwards, open crystal salt outlet, salt is dug out pack.
The above is only preferred embodiment of the present utility model; should be understood that; for those skilled in the art; under the prerequisite not departing from the utility model know-why; can also make some improvements and modifications, these improvements and modifications also should be considered as protection domain of the present utility model.
Claims (5)
1. a crystal solution demineralization plant, it is characterized in that, described equipment comprises the desalination accumulator still of the use that is used alone or connects and removes salt oven, described desalination accumulator still comprises kettle, reductor, the agitator of sealing, crystal solution entrance, crystal solution outlet and concentration analyzer, crystal solution entrance is positioned at kettle top, concentration analyzer is positioned at still near kettle top, and crystal solution outlet is positioned at the bottom of kettle, and crystal solution entrance is connected by pipeline with the discharge gate of evaporative crystallization still; Except salt oven comprises crystal solution entrance, saturated brine refluxing opening, crystal salt outlet, drain and concentration analyzer, the still top that saturated brine refluxing opening except salt oven is positioned at except salt oven is in cap shape structure, except the crystal solution entrance of salt oven is positioned at kettle upper portion side wall, except the drain of salt oven is near autoclave body bottom, except the concentration analyzer in salt oven is near kettle top, except the crystal salt outlet of salt oven is near autoclave body bottom; Except the crystal solution entrance of salt oven is connected with the discharge gate of evaporative crystallization still by crystal solution discharging pump and pipeline, or pass through crystal solution discharging pump and pipeline and export with the crystal solution of desalination accumulator still and be connected.
2. crystal solution demineralization plant as claimed in claim 1, it is characterized in that, the diameter that the described crystal salt except salt oven exports is greater than 400mm.
3. crystal solution demineralization plant as claimed in claim 1, is characterized in that, described desalination accumulator still is respectively equipped with the outside except salt oven the concentration display be connected with concentration analyzer.
4. crystal solution demineralization plant as claimed in claim 1, it is characterized in that, discharge gate and the vertical direction angle of described evaporative crystallization still are not more than 135 °.
5. crystal solution demineralization plant as claimed in claim 1, it is characterized in that, be provided with chuck at the outer wall of described evaporative crystallization still, chuck is provided with water inlet and delivery port, and water inlet is connected with heater by water pipe and water pump with delivery port.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520413567.1U CN204815761U (en) | 2015-06-16 | 2015-06-16 | Crystallization liquid desalination equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520413567.1U CN204815761U (en) | 2015-06-16 | 2015-06-16 | Crystallization liquid desalination equipment |
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| Publication Number | Publication Date |
|---|---|
| CN204815761U true CN204815761U (en) | 2015-12-02 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520413567.1U Expired - Fee Related CN204815761U (en) | 2015-06-16 | 2015-06-16 | Crystallization liquid desalination equipment |
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| CN (1) | CN204815761U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108480297A (en) * | 2018-03-12 | 2018-09-04 | 中国科学院上海硅酸盐研究所 | Historical relic removes salt well |
-
2015
- 2015-06-16 CN CN201520413567.1U patent/CN204815761U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108480297A (en) * | 2018-03-12 | 2018-09-04 | 中国科学院上海硅酸盐研究所 | Historical relic removes salt well |
| CN108480297B (en) * | 2018-03-12 | 2020-12-11 | 中国科学院上海硅酸盐研究所 | Cultural relic desalting well |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20151202 Termination date: 20160616 |