CN203447809U - MVR (Mechanical Vapor Recompression) evaporative crystallization system - Google Patents
MVR (Mechanical Vapor Recompression) evaporative crystallization system Download PDFInfo
- Publication number
- CN203447809U CN203447809U CN201320405273.5U CN201320405273U CN203447809U CN 203447809 U CN203447809 U CN 203447809U CN 201320405273 U CN201320405273 U CN 201320405273U CN 203447809 U CN203447809 U CN 203447809U
- Authority
- CN
- China
- Prior art keywords
- evaporimeter
- crystallizer
- heat exchanger
- crystallization system
- solution
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model provides an MVR (Mechanical Vapor Recompression) evaporative crystallization system. The MVR evaporative crystallization system comprises a steam-liquid separator, an evaporator, a steam compressor, a crystallizer, a heat exchanger I and a vacuum pump which are connected by pipelines and related pumps, wherein a heat exchanger II is arranged between the evaporator and the crystallizer; the crystallizer is internally provided with a cooler. According to the MVR evaporative crystallization system, the heat exchanger device is arranged between the evaporator and the crystallizer and a solution cooled by the crystallizer is used for cooling a hot solution to be cooled and a solution to be cooled is used for heating the cooled solution, so that the consumption of cooling water and heating energy is saved. The MVR evaporative crystallization system is simple in structure, small in investment, low in cost and obvious in energy-saving effect.
Description
Technical field
The utility model relates to a kind of MVR evaporation and crystallization system, the evaporative crystallization field of rising and increasing with temperature in particular for solute solubility.
Background technology
Because the rising of the solubility with temperature of NaCl increasess slowly, so the mode of conventional evaporative crystallization is obtained NaCl crystal.Common MVR evaporation and crystallization system has reclaimed the steam latent heat of evaporimeter and vapour liquid separator, thereby has saved energy consumption.But NaCl solution is unsuitable crystallization in evaporimeter, at evaporimeter intercrystalline, is equivalent to fouling, not only can cause the evaporimeter coefficient of heat transfer to decline to a great extent, and also can cause the problems such as pipeline obstruction.Therefore NaCl solution can only be heated to saturation state in evaporimeter, after discharge system, is further processed.
In prior art, first NaCl solution is concentrated into saturation state in evaporimeter, then it is concentrated to pass in crystallizer heating separately.But due to NaCl crystallization in crystallizer, cause heating effect variation, and in heating process, the secondary steam recovery difficult of crystallizer outlet is large, therefore causes evaporative crystallization energy consumption high.
Utility model content
In order to solve in prior art, the high technical problem of energy consumption in to this process of the further evaporative crystallization of NaCl saturated solution, the purpose of this utility model is to provide a kind of evaporation and crystallization system from the MVR of cooling/self heating function that has, this system utilizes the cooling solution of crystallizer to go cooling hot solution to be cooled, by solution to be cooled, cooling solution is heated simultaneously, thereby saved the consumption of cooling water and heat energy.
To achieve these goals, the utility model has adopted following technical scheme:
A MVR evaporation and crystallization system, comprises vapour liquid separator, evaporimeter, and the outlet of described evaporimeter is connected with vapour liquid separator, and vapour compression machine is arranged between vapour liquid separator and evaporimeter; Vavuum pump is connected with evaporimeter; The discharge outlet of evaporimeter is also provided with draining pump; Draining pump is connected with water tank by heat exchanger I; Between described evaporimeter and crystallizer, be provided with heat exchanger II, in crystallizer, be provided with cooler.
Preferably, between described evaporimeter and heat exchanger II, be provided with forced circulation pump I, between described crystallizer and heat exchanger II, be provided with forced circulation pump II.
Preferably, the vavuum pump being connected with evaporimeter, by part not condensing pass into the bottom of evaporimeter.
The beneficial effects of the utility model are:
MVR evaporation and crystallization system of the present utility model by arranging heat exchanger apparatus between evaporimeter and crystallizer, utilize the cooling solution of crystallizer to go cooling hot solution to be cooled, by hot solution to be cooled, cooling solution is heated simultaneously, thereby saved the consumption of cooling water and heat energy.System architecture is simple, drops into littlely, and cost is low, and energy-saving effect is obvious.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model;
Reference numeral
1. vapour liquid separator; 2. circulating pump; 3. evaporimeter; 4. vapour compression machine; 5. vavuum pump;
6. forced circulation pump I; 7. heat exchanger II; 8. crystallizer; 9. forced circulation pump II;
10. heat exchanger I; 11. draining pumps; 12. water tanks; 13. coolers; 14. charging apertures
The specific embodiment
Below in conjunction with accompanying drawing, preferred embodiment of the present utility model is described in further detail.
As shown in Figure 1, MVR evaporation and crystallization system of the present utility model, comprises the vapour liquid separator 1, evaporimeter 3 and the crystallizer 8 that by pipeline, are connected with associated pump, and vapour compression machine 4 is arranged between vapour liquid separator 1 and evaporimeter 3;
The outlet of vapour liquid separator 1 bottom is connected with the entrance of evaporimeter 3 by circulating pump 2;
The outlet of evaporimeter 3 is connected with vapour liquid separator 1;
Vavuum pump 5 is connected with evaporimeter 3, and the discharge outlet of evaporimeter 3 is also provided with draining pump 11;
Draining pump 11 is connected with water tank 12 by heat exchanger I 10;
Between described evaporimeter 3 and crystallizer 8, be provided with heat exchanger II 7, between described evaporimeter 3 and heat exchanger II 7, be provided with forced circulation pump I 6, between described crystallizer 8 and heat exchanger II 7, be provided with forced circulation pump II 9;
In crystallizer 8, be provided with cooler 13;
Crystallizer 8 is connected with vapour liquid separator 1 through forced circulation pump II 9, heat exchanger II 7 and heat exchanger I 10 successively;
Evaporimeter 3 is connected with crystallizer 8 with heat exchanger II 7 through forced circulation pump I 6 successively.
During concrete enforcement, raw material passes in vapour liquid separator 1 from charging aperture 14, and the solution of vapour liquid separator 1 bottom is squeezed in evaporimeter 3 by circulating pump 2.The outlet of evaporimeter 3 connects vapour liquid separator 1, completes after vapour, liquid separation in vapour liquid separator 1, and steam passes into vapour compression machine 4, and after compression, the temperature and pressure of steam rises, and passes into evaporimeter 3 and carries out heat exchange, as the power of evaporimeter 3 evaporations.
When the solution concentration in device 3 to be evaporated reaches discharge opeing and requires, open forced circulation pump I 6, the solution major part not being evaporated in evaporimeter 3 is returned in vapour liquid separator 1 by pipeline, part solution, by forced circulation pump I 6 and heat exchanger II 7, enters crystallizer 8, when the solution in device 8 to be crystallized reaches certain liquid level requirement, close forced circulation pump I 6, start cooler 13, the interior solution temperature of device 8 to be crystallized is down to when temperature required, closes cooler 13.Open forced circulation pump II 9, after a period of time, open forced circulation pump I 6.From the cold soln of the hot solution of evaporimeter 3 interior outflows and outflow from crystallizer 8, the cooling and preheating realizing respectively in heat exchanger II 7.In this process, answer the temperature of the interior cold soln outlet of Real-Time Monitoring crystallizer 8, if it is temperature required to maintain crystallizer 8 outlets by the natural type of cooling, start cooler 13, now only need a small amount of cooling water.
The cold soln flowing out from crystallizer 8 is after 7 preheatings of heat exchanger II, and the further heat exchange of condensed water exporting with evaporimeter 3 in heat exchanger I 10, then passes in vapour liquid separator 1 and enter next circulation, and condensed water passes into water tank 12.
In this process, the vavuum pump 5 being connected with evaporimeter 3 by part not condensing pass into the bottom of evaporimeter 3, to regulate evaporimeter 3 inner fluid disturbances, thereby regulate heat exchange amount.
Obviously, MVR evaporation and crystallization system of the present utility model, can also be for the crystallization processes of the materials such as sodium nitrate (NaNO3), ammonium chloride (NH4Cl) and potassium chloride (KCl) except the crystallization processes for sodium chloride (NaCl).
As mentioned above, MVR evaporation and crystallization system of the present utility model by arranging heat exchanger apparatus between evaporimeter and crystallizer, utilize the cooling solution of crystallizer to go cooling hot solution to be cooled, by hot solution to be cooled, cooling solution is heated simultaneously, thereby saved the consumption of cooling water and heat energy.System architecture is simple, drops into littlely, and cost is low, and energy-saving effect is obvious.
Finally explanation is, above embodiment is only unrestricted in order to the technical solution of the utility model to be described, although the utility model is had been described in detail with reference to preferred embodiment, those of ordinary skill in the art is to be understood that, can modify or be equal to replacement the technical solution of the utility model, and not departing from aim and the scope of technical solutions of the utility model, it all should be encompassed in the middle of claim scope of the present utility model.
Claims (3)
1. a MVR evaporation and crystallization system, comprises vapour liquid separator (1), evaporimeter (3), and the outlet of described evaporimeter (3) is connected with vapour liquid separator (1), and vapour compression machine (4) is arranged between vapour liquid separator (1) and evaporimeter (3); Vavuum pump (5) is connected with evaporimeter (3), and the discharge outlet of evaporimeter (3) is also provided with draining pump (11); Draining pump (11) is connected with water tank (12) by heat exchanger I (10); It is characterized in that: between described evaporimeter (3) and crystallizer (8), be provided with heat exchanger II (7), in crystallizer (8), be provided with cooler (13).
2. MVR evaporation and crystallization system according to claim 1, it is characterized in that, between described evaporimeter (3) and heat exchanger II (7), be provided with forced circulation pump I (6), between described crystallizer (8) and heat exchanger II (7), be provided with forced circulation pump II (9).
3. MVR evaporation and crystallization system according to claim 1, is characterized in that, the vavuum pump (5) being connected with evaporimeter (3), by part not condensing pass into the bottom of evaporimeter (3).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320405273.5U CN203447809U (en) | 2013-07-05 | 2013-07-05 | MVR (Mechanical Vapor Recompression) evaporative crystallization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320405273.5U CN203447809U (en) | 2013-07-05 | 2013-07-05 | MVR (Mechanical Vapor Recompression) evaporative crystallization system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203447809U true CN203447809U (en) | 2014-02-26 |
Family
ID=50127714
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320405273.5U Expired - Lifetime CN203447809U (en) | 2013-07-05 | 2013-07-05 | MVR (Mechanical Vapor Recompression) evaporative crystallization system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203447809U (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103896310A (en) * | 2014-03-19 | 2014-07-02 | 中国恩菲工程技术有限公司 | Preparation method of lithium sulfate purified concentrate |
| CN103896311A (en) * | 2014-03-19 | 2014-07-02 | 中国恩菲工程技术有限公司 | Production equipment of lithium sulfate purified concentrated solution |
| CN104258583A (en) * | 2014-10-28 | 2015-01-07 | 湖州核源机械设备有限公司 | MVR evaporator and evaporation method |
| CN104399266A (en) * | 2014-11-05 | 2015-03-11 | 广州市心德实业有限公司 | MVR evaporation device and partial pressure evaporation method |
| CN104524807A (en) * | 2015-01-25 | 2015-04-22 | 陈式好 | MVR (Mechanical Vapor Recompression) continuous evaporating crystallizing system |
| CN104548651A (en) * | 2015-01-19 | 2015-04-29 | 陈式好 | Industrial grade energy-saving and water-saving type MVR (mechanical vapor recompression) continuous evaporative crystallization system |
| CN107098364A (en) * | 2017-04-17 | 2017-08-29 | 安徽广信农化股份有限公司 | A kind of purifying technique of pyraclostrobin by-product sodium bromide |
-
2013
- 2013-07-05 CN CN201320405273.5U patent/CN203447809U/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103896310A (en) * | 2014-03-19 | 2014-07-02 | 中国恩菲工程技术有限公司 | Preparation method of lithium sulfate purified concentrate |
| CN103896311A (en) * | 2014-03-19 | 2014-07-02 | 中国恩菲工程技术有限公司 | Production equipment of lithium sulfate purified concentrated solution |
| CN104258583A (en) * | 2014-10-28 | 2015-01-07 | 湖州核源机械设备有限公司 | MVR evaporator and evaporation method |
| CN104399266A (en) * | 2014-11-05 | 2015-03-11 | 广州市心德实业有限公司 | MVR evaporation device and partial pressure evaporation method |
| CN104548651A (en) * | 2015-01-19 | 2015-04-29 | 陈式好 | Industrial grade energy-saving and water-saving type MVR (mechanical vapor recompression) continuous evaporative crystallization system |
| CN104524807A (en) * | 2015-01-25 | 2015-04-22 | 陈式好 | MVR (Mechanical Vapor Recompression) continuous evaporating crystallizing system |
| CN107098364A (en) * | 2017-04-17 | 2017-08-29 | 安徽广信农化股份有限公司 | A kind of purifying technique of pyraclostrobin by-product sodium bromide |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN203447809U (en) | MVR (Mechanical Vapor Recompression) evaporative crystallization system | |
| CN203355317U (en) | Four-effect crystallizing evaporator | |
| CN104692575A (en) | Crystallization treatment method and device of high salt wastewater | |
| CN203428931U (en) | Concentration and crystallization equipment for ammonium chloride | |
| CN204897422U (en) | Ammonium chloride solution evaporation crystal system | |
| US11353242B2 (en) | Semi-open high-temperature heat pump system and working method thereof | |
| CN201954828U (en) | Efficient and energy-saving lithium bromide refrigerator | |
| CN206414788U (en) | A kind of salting liquid saves evaporating, concentrating and crystallizing system | |
| CN104567079A (en) | Hot water type lithium bromide absorption water chilling unit | |
| CN103983046B (en) | The board-like full liquid generator of width passage and falling-film absorber and ammonia water absorption refrigerating machine | |
| CN102914081A (en) | Two-section flue gas hot-water single/double-effect composite lithium bromide absorption type refrigerating unit | |
| CN104313267A (en) | Device for realizing salt and water recycling by utilizing salt quenching waste heat | |
| CN113310246A (en) | Wine condensation heat energy comprehensive utilization system and heat energy comprehensive utilization method | |
| CN206138765U (en) | Energy -conserving vaporization system of calcium nitrate solution | |
| CN203893505U (en) | Wide channel and narrow channel plate type hydraulic filling generator, wide channel and narrow channel plate type falling film absorber and ammonia absorption refrigerator | |
| CN204999762U (en) | Concentrated crystallization equipment of carnallite waste water | |
| CN104567442B (en) | Blast furnace slag flushing water waste heat refrigerating system | |
| CN208603748U (en) | A kind of water treatment vaporization system | |
| CN108609786B (en) | Evaporation condensation circulation equipment and method for driving brine separation and full recovery of high-salt wastewater by low-quality waste heat | |
| CN103394204A (en) | Acid bath multi-effect liquid film evaporating process and device | |
| CN202973647U (en) | Flue gas hot water single/double-effect composite lithium bromide absorption refrigerating unit | |
| CN205627127U (en) | MVR triple -effect evaporator | |
| CN204373260U (en) | Hot water type lithium bromide absorption water chilling unit | |
| CN210663439U (en) | High-temperature wastewater lithium bromide absorption refrigeration all-in-one machine | |
| CN204824178U (en) | Monoammonium phosphate solution evaporation crystallization equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20140226 |