CN204932926U - A kind of zero-emission evaporation crystallization equipment - Google Patents
A kind of zero-emission evaporation crystallization equipment Download PDFInfo
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- CN204932926U CN204932926U CN201520536553.9U CN201520536553U CN204932926U CN 204932926 U CN204932926 U CN 204932926U CN 201520536553 U CN201520536553 U CN 201520536553U CN 204932926 U CN204932926 U CN 204932926U
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Abstract
The utility model relates to a kind of zero-emission evaporation crystallization equipment, and it comprises preheating device, vaporising device, Crystallization Separation device and tail gas condensation device.Evaporation crystallization equipment described in the utility model instead of traditional Steam Heating evaporation and crystallization mode, adopt the indirect steam that compressor compresses vaporising device evaporates, indirect steam after using pressurization to heat up is as heating steam, and realize Inner eycle by arranging loop, accomplish without the need to external Steam Heating, without the need to water condensation, a small amount of electric energy is only needed just to realize good evaporation effect, and realize clean tail gas, thus both for reducing costs in evaporation process process, economize energy opens up a kind of new way, realizes clean environment firendly again.
Description
Technical field
The utility model relates to the evaporating, concentrating and crystallizing technical field of solution, is specifically related to a kind of evaporation crystallization equipment of zero-emission.
Background technology
Industrial material and industrial wastewater often adopt evaporating and concentrating process, and steam consumption is high, and raw material is very serious to the corrosion of equipment.Based on this, adopt evaporation technology to evaporate, equipment material selects suitable resistant material, and problem can be given and solution.In evaporation technique, the form evaporator of multiple-effect evaporation adopts comparatively general.But in recent years, along with the rise at full speed of steam price, the energy consumption of this kind of evaporation process also makes vast business burden sharply increase, and often occur exhaust emissions problem in evaporation, both wasted heats, cause environmental pollution again.
Utility model content
In order to overcome the deficiencies in the prior art, the purpose of this utility model is to provide a kind of zero-emission evaporation crystallization equipment, by the self-loopa between main heat exchanger and separator, adopt the indirect steam that compressor compresses crystal separator gives off, use the indirect steam after compression to use as heating steam, realize the object of evaporation and concentration, thus economize energy, reduce costs, enhance productivity.
For solving the problem, the technical scheme that the utility model adopts is as follows:
A kind of zero-emission evaporation crystallization equipment, it comprises preheating device, vaporising device, Crystallization Separation device and tail gas condensation device;
Described preheating device comprises material buffer tank and preheater, and material enters material buffer tank and pumps in preheater through conveying pipeline and carry out preheating;
Described vaporising device comprises main heat exchanger, separator, vapour compression machine and chilled water tank, wherein, the discharge end of preheater is connected on the feed end of main heat exchanger after condensing heat exchanger, main heat exchanger is connected with separator and forms closed-loop path, described closed-loop path is provided with circulating pump, material after preheating is circulated in main heat exchanger and separator by circulating pump, constantly isolate the concentrate of steam and high saturation, especially, between the steam (vapor) outlet of described separator and main heat exchanger, also vapour compression machine is set, the steam that separator is separated enters vapour compression machine adiabatic compression, reenter main heat exchanger cycle heat exchange, chilled water tank is entered after being condensed into water, chilled water tank is connected on the condensation-water drain of main heat exchanger by water-supply-pipe,
Described Crystallization Separation device comprises crystallizer and sedimentator device, and crystallizer and sedimentator device are connected to the discharge end of separator in turn by a discharging pump, and the concentrate reaching hypersaturated state pumps into crystallizer crystallization, and isolates crystal through sedimentator device;
Chilled water tank is connected by pipeline by described tail gas condensation device gets back to preheater and condensing heat exchanger, after completing preheating and condensing heat-exchange, discharges cooling water.
The utility model can also pass through following scheme implementation:
Preferred scheme is had as one of the present utility model, described main heat exchanger and separator connect and compose a closed-loop path by pipeline, pipeline is provided with a circulating pump, solution material after preheating enters main heat exchanger and heating steam heat exchange, the solution material obtaining heat enters separator flash separation and goes out indirect steam and concentrate, concentrate reenters closed-loop path by circulating pump effect, constantly through main heat exchanger and separator flash separation effect, finally reach hypersaturated state and pump into crystallizer from separator and carry out crystallization.
Preferred scheme is had as one of the present utility model, described chilled water tank is provided with coolant outlet and not solidifying offgas outlet, coolant outlet is connected on preheater after a distilled water pump, the cooling water that chilled water tank is discharged provides heat exchange thermal source through preheater, not solidifying offgas outlet is connected on condensing heat exchanger through pipeline, and the not solidifying tail gas that chilled water tank is discharged enters after condensing heat exchanger carries out heat exchange condensation discharges.
Have preferred scheme as one of the present utility model, connected by conveying pipeline between described material buffer tank and preheater, conveying pipeline is provided with feed pump, and material exports from material buffer tank, pumps into preheater carry out preheating through feed pump.
Have preferred scheme as one of the present utility model, described sedimentator device and be provided with second servo loop between separator, second servo loop is provided with mother liquor pump, and the mother liquor obtained after sedimentator is pumped in separator through mother liquor and circulates.
There is preferred scheme as one of the present utility model, the not solidifying tail gas mouth in described chilled water tank, by being connected with a condensing heat exchanger, wherein will be able to condensation cleaning by steam by heat exchange.
Compared to existing technology, the beneficial effects of the utility model are: zero-emission evaporation crystallization equipment described in the utility model instead of traditional steam-heated evaporation and crystallization mode, adopt the indirect steam that compressor compresses crystallizer gives off, use the indirect steam after compression as heating steam, and the circulation of equipment self is achieved by arranging loop, accomplish without the need to raw Steam Heating, without the need to condensing plant, only need a small amount of electric energy just can reach the effect of good evaporation, thus reduce costs in solution-treated process, economize energy opens a new way.
Below in conjunction with the drawings and specific embodiments, the utility model is described in further detail.
Accompanying drawing explanation
Fig. 1 is the structural representation of the utility model preferred embodiment.
Detailed description of the invention
As shown in Figure 1, zero-emission evaporation crystallization equipment described in the utility model, it comprises preheating device, vaporising device, Crystallization Separation device and tail gas condensation device;
Described preheating device comprises material buffer tank 1, preheater 3, and material buffer tank 1 is connected by one section of conveying pipeline with preheater 3, described conveying pipeline is provided with feed pump 2;
Described vaporising device comprises main heat exchanger 4, separator 5, vapour compression machine 6 and chilled water tank 8; The discharge end of the condensing heat exchanger 10 after the feed end connection preheater 3 of described main heat exchanger 4; Separator 5 is connected with main heat exchanger 4 and forms closed-loop path, described closed-loop path is provided with circulating pump 7, concentrate after separator 5 is separated is entered into separator 5 again after being entered by circulating pump 7 in main heat exchanger 4 and evaporating and isolates concentrate, and concentrate is circulated between main heat exchanger 4 and separator 5 by closed-loop path; The steam (vapor) outlet of described separator 5 connects the air inlet of vapour compression machine 6 by one section of appendix, the gas outlet of vapour compression machine 6 is communicated with main heat exchanger 4, and the condensation-water drain of main heat exchanger 4 connects chilled water tank 8 by water-supply-pipe;
Described Crystallization Separation device comprises crystallizer 12, sedimentator device 13, and crystallizer 12 and sedimentator device 13 are connected to the discharge end of separator in turn by a discharging pump 11.
Adopt device condensing crystallizing evaporation technology described in the utility model as follows: to regulate the temperature in material surge tank 1 to be room temperature, sodium chloride stoste pumps into preheater 3 through feed pump 2, heat exchange is produced with preheater 3, after preheater 3, temperature rises, then with the not solidifying tail gas heat exchange in condensing heat exchanger 10 in chilled water tank 8; Solution after preheating enters into main heat exchanger 4, and circulated in main heat exchanger 4 and separator 5 by circulating pump 7, with heating steam heat exchange in main heat exchanger 4, the solution absorbing heat enters flash distillation in separator 5, and isolate indirect steam and concentrate, indirect steam enters vapour compression machine 6 from separator 5 steam (vapor) outlet, and after the adiabatic compression of vapour compression machine 6, temperature and pressure gets a promotion; Indirect steam after increasing temperature and pressure enters main heat exchanger 4 and solution heat exchange as heating steam, is condensed into water, and enters chilled water tank 8 after heat release; The solution absorbing heat enters flash distillation in separator 5 and isolates indirect steam and concentrate, pumps into crystallization in crystallizer 12, then isolate crystal through crystallizer 12 and sedimentator device 13 when the concentration of solution reaches hypersaturated state through discharging pump 11; Can reuse or qualified discharge from the last cooling water out of preheater.
The utility model can also pass through following scheme implementation:
Have preferred scheme as one of the present utility model, described chilled water tank 8 is provided with coolant outlet, and the water inlet end of a distilled water pump 9 is connected to the coolant outlet of chilled water tank 8 by water-supply-pipe, and the water side of distilled water pump 9 is connected on preheater 3.Because water out also has uniform temperature from chilled water tank 8, if directly discharge can cause the waste of thermal source, the water in chilled water tank 8 is incorporated in preheater 3, as the thermal source of preheater 3, thus the object making full use of heat can be reached.
Have preferred scheme as one of the present utility model, described sedimentator device 13 and be provided with loop between separator 5, loop is provided with mother liquor pump 14, the mother liquor obtained after sedimentator through mother liquor pump 14 be sent in separator 5 circulate.Mother liquor after separation is saturated solution, direct discharge may cause resource reclaim incomplete, discharge after stain environment, therefore after designing second servo loop, mother liquor enters into separator by second servo loop, and then between separator and main heat exchanger, circulation is concentrated, to reach after predetermined concentration Crystallization Separation again, circulation like this, finally realizes evaporation and reclaims completely.
Have preferred scheme as one of the present utility model, the condensation-water drain of described preheater 3 is connected with outlet pipe.The condensed water eventually passed after preheater hot exchange is discharged through outlet pipe.
Have preferred scheme as one of the present utility model, the fixed gas outlet of described chilled water tank 8 is connected with water pipe, and water pipe end is connected with condensing heat exchanger 10, and the fixed gas after condensing heat exchanger 10 heat exchange is cleaned discharge, energy-conservation environmental protection again.
Above-mentioned embodiment is only preferred embodiment of the present utility model; can not limit the scope of the utility model protection with this, change and the replacement of any unsubstantiality that those skilled in the art does on basis of the present utility model all belong to the utility model scope required for protection.
Claims (5)
1. a zero-emission evaporation crystallization equipment, comprises preheating device, vaporising device, Crystallization Separation device and tail gas condensation device, it is characterized in that:
Described preheating device comprises material buffer tank and preheater, and solution material enters material buffer tank and pumps in preheater through conveying pipeline and carry out preheating;
Described vaporising device comprises main heat exchanger, separator, vapour compression machine and chilled water tank, wherein, the discharge end of preheater is connected on the feed end of main heat exchanger after condensing heat exchanger, main heat exchanger is connected with separator and forms closed-loop path, solution material after preheating in closed-loop path cocycle through main heat exchanger and separator, constantly isolate the concentrate of steam and high saturation, between the steam (vapor) outlet of described separator and main heat exchanger, also vapour compression machine is set, the steam that separator is separated enters vapour compression machine adiabatic compression, reenter main heat exchanger cycle heat exchange, steam-condensation Cheng Shuihou enters chilled water tank, chilled water tank is connected on the condensation-water drain of main heat exchanger by water-supply-pipe,
Described Crystallization Separation device comprises crystallizer and sedimentator device, and crystallizer and sedimentator device are connected to the discharge end of separator in turn by a discharging pump, and the concentrate reaching hypersaturated state pumps into crystallizer crystallization, and isolates crystal through sedimentator device;
Chilled water tank is connected by pipeline by described tail gas condensation device gets back to preheater and condensing heat exchanger, after completing preheating and condensing heat-exchange, discharges cooling water.
2. a kind of zero-emission evaporation crystallization equipment according to claim 1, it is characterized in that: described main heat exchanger and separator connect and compose a closed-loop path by pipeline, pipeline is provided with a circulating pump, solution material after preheating enters main heat exchanger and heating steam heat exchange, the solution material obtaining heat enters separator flash separation and goes out indirect steam and concentrate, concentrate reenters closed-loop path by circulating pump effect, constantly through main heat exchanger and separator flash separation effect, finally reach hypersaturated state and pump into crystallizer from separator and carry out crystallization.
3. a kind of zero-emission evaporation crystallization equipment according to claim 1, it is characterized in that: described chilled water tank is provided with coolant outlet and not solidifying offgas outlet, coolant outlet is connected on preheater after a distilled water pump, the cooling water that chilled water tank is discharged provides heat exchange thermal source through preheater, not solidifying offgas outlet is connected on condensing heat exchanger through pipeline, and the not solidifying tail gas that chilled water tank is discharged enters after condensing heat exchanger carries out heat exchange condensation discharges.
4. a kind of zero-emission evaporation crystallization equipment according to claim 1, it is characterized in that: connected by conveying pipeline between described material buffer tank and preheater, conveying pipeline is provided with feed pump, and material exports from material buffer tank, pumps into preheater carry out preheating through feed pump.
5. a kind of zero-emission evaporation crystallization equipment according to claim 1, is characterized in that: be provided with loop between described sedimentator device and separator, loop is provided with mother liquor pump, and the mother liquor obtained after sedimentator is pumped in separator through mother liquor and circulates.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520536553.9U CN204932926U (en) | 2015-07-22 | 2015-07-22 | A kind of zero-emission evaporation crystallization equipment |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201520536553.9U CN204932926U (en) | 2015-07-22 | 2015-07-22 | A kind of zero-emission evaporation crystallization equipment |
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| CN204932926U true CN204932926U (en) | 2016-01-06 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105031965A (en) * | 2015-07-22 | 2015-11-11 | 深圳市捷晶能源科技有限公司 | Zero-emission evaporation and crystallization device |
| CN106698493A (en) * | 2017-01-05 | 2017-05-24 | 四川理工学院 | Evaporative crystallization technology of barium chloride |
| CN110433508A (en) * | 2019-08-21 | 2019-11-12 | 中国科学院广州能源研究所 | A kind of compensation vapor recompression system of accumulation of heat and its it is concentrated by evaporation processing method |
-
2015
- 2015-07-22 CN CN201520536553.9U patent/CN204932926U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105031965A (en) * | 2015-07-22 | 2015-11-11 | 深圳市捷晶能源科技有限公司 | Zero-emission evaporation and crystallization device |
| CN106698493A (en) * | 2017-01-05 | 2017-05-24 | 四川理工学院 | Evaporative crystallization technology of barium chloride |
| CN110433508A (en) * | 2019-08-21 | 2019-11-12 | 中国科学院广州能源研究所 | A kind of compensation vapor recompression system of accumulation of heat and its it is concentrated by evaporation processing method |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: A1701-1707, building 12, shenzhenwan science and technology ecological park, No.18, South Keji Road, high tech community, Yuehai street, Nanshan District, Shenzhen, Guangdong 518000 Patentee after: Shenzhen Jiejing Technology Co.,Ltd. Address before: 518000 zone B, floor 2, building A3, Shenzhen digital technology park, Gaoxin South 7th Road, high tech Zone South, Nanshan District, Shenzhen, Guangdong Province Patentee before: SHENZHEN CRYSTAL ENERGY TECH Co.,Ltd. |
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| CP03 | Change of name, title or address | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: A zero emission evaporative crystallization equipment Effective date of registration: 20220705 Granted publication date: 20160106 Pledgee: Shenzhen hi tech investment small loan Co.,Ltd. Pledgor: Shenzhen Jiejing Technology Co.,Ltd. Registration number: Y2022980009855 |
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| PE01 | Entry into force of the registration of the contract for pledge of patent right |