CN104399266B - A kind of MVR vaporising device and partial pressure evaporation method - Google Patents
A kind of MVR vaporising device and partial pressure evaporation method Download PDFInfo
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- CN104399266B CN104399266B CN201410620982.4A CN201410620982A CN104399266B CN 104399266 B CN104399266 B CN 104399266B CN 201410620982 A CN201410620982 A CN 201410620982A CN 104399266 B CN104399266 B CN 104399266B
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Abstract
The present invention relates to a kind of MVR vaporising device, including preevaporator, crystallizing evaporator, the first compressor and the second compressor, the import and export of described first compressor connects indirect steam outlet and the entrance of preevaporator respectively, and described second compressor is positioned on the indirect steam loop of crystallizing evaporator.Owing to the concentration concentration of fractional crystallization device is high, indirect steam requires that the temperature rise reached is the highest after compression, the indirect steam of the present invention is through dividing potential drop, the indirect steam making entrance fractional crystallization device is individually compressed by the second compressor, it individually enters the second compressor, and the indirect steam of pre-concentration is heated up by the first compressor compresses, enters a compressor relative to steam total head, greatly reduce the flow to compressor and temperature increase requirement, thus reduce cost and run the purpose of power consumption.The invention still further relates to the partial pressure evaporation method of above-mentioned vaporising device.The present invention is applicable to may be used for big evaporation capacity, the concentration and evaporation of high boiling point feed liquid.
Description
Technical field
The present invention relates to liquid concentration field, particularly a kind of MVR vaporising device and partial pressure evaporation method.
Background technology
MVR(Mechanical Vapor Recompression function of mechanical steam recompression) operation principle is by machinery
The steam of the low-pressure low-temperature that vaporizer is steamed by the compressor driven, is compressed to elevated pressures and temperature, becomes the steaming of high-temperature position
Vapour, as heater, reboiler and vaporizer thermal source, has i.e. reclaimed the indirect steam latent heat of vaporization, thus has saved energy consumption.But
It is that, for evaporated crystallization device, evaporation capacity is the biggest and the feed liquid elevation of boiling point is the biggest, and the burden requirement to compressor is the highest,
Its cost the most just steeply rises with power consumption.
In prior art, during the feed liquid that evaporative crystallization evaporation capacity is big and the elevation of boiling point is big, such as low concentration ammonium chloride wastewater, its
MVR evaporation and crystallization system the most first carries out prevapourising and improves concentration, and re-evaporation crystallizes thus improves concentration further, MVR unit
Use the mode of two-stage compressor total head series connection, the indirect steam from prevapourising and evaporative crystallization is compressed, compressor
Carry the big evaporation capacity of whole vapo(u)rization system, add the high temperature rise requirement to compressor, thus result in evaporative crystallization
High cost and highly energy-consuming.
Summary of the invention
In order to overcome above-mentioned technical problem, it is an object of the invention to provide a kind of MVR cost-effective, reduction energy consumption and steam
Transmitting apparatus.
The technical solution adopted in the present invention is:
A kind of MVR vaporising device, including preevaporator, crystallizing evaporator, the first compressor and the second compressor, described the
The import and export of one compressor connects indirect steam outlet and the entrance of preevaporator respectively, and described second compressor is positioned at evaporation
On the indirect steam loop of crystallizer.
As the further improvement of technique scheme, the import and export of described second compressor connects evaporative crystallization respectively
The indirect steam outlet of device and entrance.
As the further improvement of technique scheme, the indirect steam outlet of described crystallizing evaporator connects the first compression
The entrance of machine, the import of described second compressor connects the outlet of the first compressor, and the outlet of described second compressor connects steams
Send out the indirect steam entrance of crystallizer.
As the further improvement of technique scheme, the concentrated solution circulation line of described preevaporator is provided with circulation
Pump, the inlet of described crystallizing evaporator connects circulation delivery side of pump by pipeline.
As the further improvement of technique scheme, described crystallizing evaporator is forced-circulation evaporation crystallizer, including
Heat exchanger, fractional crystallization device and forced circulation pump, the inlet of described heat exchanger as the inlet of crystallizing evaporator, described in change
The liquid outlet of hot device is connected by pipeline with the inlet of fractional crystallization device, and described forced circulation pump is positioned at the inlet of heat exchanger
With between the liquid outlet of fractional crystallization device, the indirect steam of described crystallizing evaporator exports at fractional crystallization device top, and entrance exists
On heat exchanger.
As the further improvement of technique scheme, described preevaporator is falling film evaporator, including evaporator body,
The gas-liquid separation chamber being connected with evaporator body, described first compressor connects gas-liquid separation chamber and evaporator body, described steaming
Send out and be connected with circulating pump by pipeline between the circulation fluid import of device bodies top and the circulation fluid outlet of bottom, constitute prevapourising
The concentrated solution circulation line of device.
Invention additionally discloses a kind of partial pressure evaporation method using above-mentioned vaporising device, it the technical scheme is that
A kind of partial pressure evaporation method, by MVR technique make feed liquid material first at preevaporator pre-concentration, after by crystallizing evaporator
Condensing crystallizing further, in pre-concentration, the indirect steam of circulation is heated up by the first compressor compresses, two circulated in condensing crystallizing
Secondary steam is heated up by the second compressor compresses before entering crystallizing evaporator.
As the further improvement of technique scheme, the indirect steam produced in condensing crystallizing is independent by the second compressor
Compression heats up.
As the further improvement of technique scheme, the indirect steam produced in condensing crystallizing is successively by the first compressor
Heat up with the second compressor compresses.
The invention has the beneficial effects as follows: owing to the concentration concentration of fractional crystallization device is high, indirect steam requires to reach after compression
The temperature rise arrived is relatively the highest, and the indirect steam of the present invention through dividing potential drop, makes the indirect steam of entrance fractional crystallization device individually by the
Two compressors are compressed, and it individually enters the second compressor, and the indirect steam of pre-concentration is heated up by the first compressor compresses,
Enter a compressor relative to steam total head, greatly reduce the flow to compressor and temperature increase requirement, thus reduce
Cost and the purpose of operation power consumption.
Accompanying drawing explanation
The present invention is further described with embodiment below in conjunction with the accompanying drawings.
Fig. 1 is the schematic diagram of first embodiment of the invention；
Fig. 2 is the schematic diagram of second embodiment of the invention.
Detailed description of the invention
MVR vaporising device as depicted in figs. 1 and 2, including preevaporator, crystallizing evaporator, the first compressor 1 and second
Compressor 2, the import and export of the first compressor 1 connects indirect steam outlet and entrance, second compressor 2 of preevaporator respectively
It is positioned on the indirect steam loop of crystallizing evaporator.
Preevaporator is falling film evaporator 6, including evaporator body 61, the gas-liquid separation chamber that is connected with evaporator body 61
62, the first compressor 1 connects gas-liquid separation chamber 62 and the top of evaporator body 61, and secondary gas-liquid separation chamber 62 separated steams
Heating in Returning evaporimeter body 61 after vapour pressure contracting intensification.The circulation fluid import at evaporator body 61 top and the circulation fluid of bottom
It is connected with circulating pump 3 by pipeline between outlet, constitutes the concentrated solution circulation line of falling film evaporator 6.Reaching next step work
Before the concentration of skill, concentrated solution, through the Circulation of circulating pump 3, keeps circulation in falling film evaporator 6 and constantly concentrates.
Crystallizing evaporator is forced-circulation evaporation crystallizer 4, including heat exchanger 42, fractional crystallization device 41 and forced circulation pump
5.The inlet of heat exchanger 42 is the inlet of forced-circulation evaporation crystallizer 4, the liquid outlet of heat exchanger 42 and fractional crystallization device
The inlet of 41 is connected by pipeline.Forced circulation pump 5 is positioned at inlet and the liquid outlet of fractional crystallization device 41 of heat exchanger 42
Between, the entrance of forced circulation pump 5 connects the outlet of circulating pump 3 by pipeline simultaneously, and the concentrated solution reaching pre-concentration concentration can
To be entered in heat exchanger 42 by circulating pump 3 and forced circulation pump 5.The indirect steam of crystallizing evaporator exports at fractional crystallization device
41 tops, entrance is on heat exchanger 42 and connects the outlet of the second compressor 2.
In first embodiment as shown in Figure 1, the import and export of the first compressor 1 is directly connected to falling film evaporation by pipeline
The indirect steam outlet of device 6 and entrance, the import and export of the second compressor 2 connects the secondary of forced-circulation evaporation crystallizer 4 respectively
Steam (vapor) outlet and entrance, two compressors mutually separate unrelated, independent heat supply.
Partial pressure evaporation method in this embodiment is as follows:
A. material liquid entrance falling film evaporator 6 carries out prevapourising, and feed liquid is transmitted back to through circulating pump 3 by the outlet of its underpart
Top is again introduced into falling film evaporator 6 and is evaporated；After feed concentration and temperature reach dynamic equilibrium, circulating pump 3 transport portion
Feed liquid continues cycling through evaporation, and other parts are transported to the feed pipe of forced circulation pump 5.
B. feed liquid is transported to heat exchanger 42 and carries out heat exchange by forced circulation pump 5, and after heat exchange, feed liquid enters fractional crystallization device 41
Carry out flash distillation；Magma in fractional crystallization device 41 enters the feed pipe of forced circulation pump 5 and continues cycling through from its underpart；Magma reaches
Subsequent technique is flowed to from bottom discharge pipe after setting requirement.
C. the condensed water of falling film evaporator 6 and the cold-warm water of forced circulation heat exchanger 42 enter condensate water pot 7, condensed water warp
Condensate pump 8 is discharged or flows to subsequent technique.
In above-mentioned steps a, the indirect steam that pre-concentration produces all enters falling liquid film after the first compressor 1 compression heats up and steams
Send out device 6 as thermal source heat exchange, in step b forced-circulation evaporation crystallizer 4 condensing crystallizing produce indirect steam individually through second pressure
Contracting machine 2 compression returns forced-circulation evaporation crystallizer 4 after heating up and carries out heat exchange.
In the second embodiment as shown in Figure 2, the indirect steam outlet of crystallizing evaporator connects entering of the first compressor 1
Mouthful, the import of the second compressor 2 connects the outlet of the first compressor 1, and the outlet of the second compressor 2 connects the two of crystallizing evaporator
Secondary steam inlet.
Partial pressure evaporation method in this embodiment is as follows:
A. material liquid entrance falling film evaporator 6 carries out prevapourising, and feed liquid is transmitted back to through circulating pump 3 by the outlet of its underpart
Top is again introduced into falling film evaporator 6 and is evaporated；After feed concentration and temperature reach dynamic equilibrium, circulating pump 3 transport portion
Feed liquid continues cycling through evaporation, and other parts are transported to the feed pipe of forced circulation pump 5.
B. feed liquid is transported to heat exchanger 42 and carries out heat exchange by forced circulation pump 5, and after heat exchange, feed liquid enters fractional crystallization device 41
Carry out flash distillation；Magma in fractional crystallization device 41 enters the feed pipe of forced circulation pump 5 and continues cycling through from its underpart；Magma reaches
Subsequent technique is flowed to from bottom discharge pipe after setting requirement.
C. the condensed water of falling film evaporator 6 and the cold-warm water of forced circulation heat exchanger 42 enter condensate water pot 7, condensed water warp
Condensate pump is discharged or flows to subsequent technique.
In above-mentioned steps a and b, the indirect steam produced in pre-concentration and condensing crystallizing is the most simultaneously through the first compressor 1
After compression heats up, being partly into falling film evaporator 6 as thermal source heat exchange, another part is by the second compressor 2 recompression
Heat up, and enter forced-circulation evaporation crystallizer 4 and carry out heat exchange.
Apparatus and method in above-described embodiment are applicable to may be used for ammonium chloride (NH4Cl) evaporative crystallization technique, it is possible to
Evaporative crystallization technique for materials such as sodium chloride (NaCl) and potassium chloride (KCl).
Above example is only in order to illustrate technical scheme and unrestricted, although with reference to preferred embodiment to this
Bright it is described in detail, it will be understood by those within the art that, technical scheme can be modified
Or equivalent, without deviating from objective and the scope of technical solution of the present invention, it all should contain the claim in the present invention
In the middle of scope.
Claims (7)
1. a MVR vaporising device, it is characterised in that: include preevaporator, crystallizing evaporator, the first compressor and the second compression
Machine, the import and export of described first compressor connects indirect steam outlet and entrance, described second compressor of preevaporator respectively
Being positioned on the indirect steam loop of crystallizing evaporator, the concentrated solution circulation line of described preevaporator is provided with circulating pump, described
The inlet of crystallizing evaporator connects circulation delivery side of pump by pipeline, and described crystallizing evaporator is forced-circulation evaporation crystallization
Device, including heat exchanger, fractional crystallization device and forced circulation pump, the inlet of described heat exchanger is as the feed liquor of crystallizing evaporator
Mouthful, the liquid outlet of described heat exchanger is connected by pipeline with the inlet of fractional crystallization device, and described forced circulation pump is positioned at heat exchange
Between inlet and the liquid outlet of fractional crystallization device of device, the indirect steam of described crystallizing evaporator exports on fractional crystallization device top
Portion, entrance is on heat exchangers.
MVR vaporising device the most according to claim 1, it is characterised in that: the import and export of described second compressor connects respectively
Connect indirect steam outlet and the entrance of crystallizing evaporator.
MVR vaporising device the most according to claim 1, it is characterised in that: the indirect steam outlet of described crystallizing evaporator
Connecting the entrance of the first compressor, the import of described second compressor connects the outlet of the first compressor, described second compressor
Outlet connect crystallizing evaporator indirect steam entrance.
MVR vaporising device the most according to claim 1, it is characterised in that: described preevaporator is falling film evaporator, including
Evaporator body, the gas-liquid separation chamber being connected with evaporator body, described first compressor connects gas-liquid separation chamber and vaporizer
Body, by pipeline and circulating pump phase between circulation fluid import and the circulation fluid outlet of bottom at described evaporator body top
Even, the concentrated solution circulation line of preevaporator is constituted.
5. the partial pressure evaporation method of the vaporising device used according to any one of claim 1 to 4, it is characterised in that: logical
Crossing MVR technique makes feed liquid material first at preevaporator pre-concentration, after by the further condensing crystallizing of crystallizing evaporator, pre-concentration circulates
Indirect steam heated up by the first compressor compresses, in condensing crystallizing, the indirect steam of circulation is entering before crystallizing evaporator by the
Two compressor compresses heat up.
Partial pressure evaporation method the most according to claim 5, it is characterised in that: the indirect steam produced in condensing crystallizing is by second
Compressor individually compresses intensification.
Partial pressure evaporation method the most according to claim 5, it is characterised in that: in condensing crystallizing produce indirect steam successively by
First compressor and the second compressor compresses heat up.
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| CN105617700A (en) * | 2015-12-25 | 2016-06-01 | 河北工业大学 | Method for evaporating and concentrating high-boiling-point salt-containing solutions |
| CN105693585B (en) * | 2016-04-11 | 2018-11-20 | 中芳特纤股份有限公司 | A kind of separation N-Methyl pyrrolidone/chloroform system and method |
| CN105771304B (en) * | 2016-05-05 | 2017-11-10 | 无锡荣丰生物工程有限公司 | Monosodium glutamate two imitates countercurrent evaporation crystal system and its course of work |
| CN107198887B (en) * | 2016-09-08 | 2019-06-21 | 江苏科技大学 | A kind of steam compression system and working method |
| 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 |
| CN107376397A (en) * | 2017-06-19 | 2017-11-24 | 南京紫晶藤节能科技有限公司 | The cold and hot linkage low-temperature evaporation condensing crystallizing system and method for low boiling solution |
| CN108211395A (en) * | 2018-02-08 | 2018-06-29 | 常州瑞持机械有限公司 | For the intelligent MVR vapo(u)rization systems of fermentation |
| CN109437238A (en) * | 2018-12-29 | 2019-03-08 | 广州市迈源科技有限公司 | A kind of ammonium chloride solution processing system and ammonium chloride solution processing method |
| CN115531898A (en) * | 2022-10-10 | 2022-12-30 | 扬州永锋工业设备安装有限公司 | Environment-friendly energy-saving MVR evaporator |
| CN117771722A (en) * | 2024-02-27 | 2024-03-29 | 江苏嘉泰蒸发设备股份有限公司 | Skid-mounted MVR evaporation crystallization equipment |
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| CN204261367U (en) * | 2014-11-05 | 2015-04-15 | 广州市心德实业有限公司 | A kind of MVR vaporising device |
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| CN202038886U (en) * | 2011-05-03 | 2011-11-16 | 深圳市瑞升华科技有限公司 | Treatment system for high-concentration industrial ammonia-nitrogen waste water |
| CN202924774U (en) * | 2012-07-18 | 2013-05-08 | 如皋市金陵化工有限公司 | Wastewater treatment system |
| CN103007553B (en) * | 2012-12-05 | 2015-11-11 | 中国科学院理化技术研究所 | A kind of function of mechanical steam recompression continuous evaporative crystallization system and method |
| CN103203116B (en) * | 2013-04-24 | 2015-09-16 | 江苏科化节能环保设备有限公司 | A kind of MVR continuous evaporative crystallization system and continuous evaporative crystallization method |
| CN203447809U (en) * | 2013-07-05 | 2014-02-26 | 重庆江增船舶重工有限公司 | MVR (Mechanical Vapor Recompression) evaporative crystallization system |
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Denomination of invention: MVR evaporation device and partial pressure evaporation method Effective date of registration: 20220311 Granted publication date: 20160831 Pledgee: Bank of China Limited by Share Ltd. Guangzhou Panyu branch Pledgor: GUANGZHOU SCHIN-TECH INDUSTRIAL Co.,Ltd. Registration number: Y2022980002459 |