CN202849193U - Multistage vacuum distillation seawater desalting device - Google Patents

Multistage vacuum distillation seawater desalting device Download PDF

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CN202849193U
CN202849193U CN2012200687208U CN201220068720U CN202849193U CN 202849193 U CN202849193 U CN 202849193U CN 2012200687208 U CN2012200687208 U CN 2012200687208U CN 201220068720 U CN201220068720 U CN 201220068720U CN 202849193 U CN202849193 U CN 202849193U
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seawater
fresh
evaporator
fresh water
water
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李星煜
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李星煜
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    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124Water desalination

Abstract

The utility model relates to a multistage vacuum distillation seawater desalting device, comprising a plurality of stages of falling film evaporators, interstage flow regulating valves, fresh water tanks, vaccumizing devices, concentrated seawater pumps, fresh water pumps and seawater delivery pumps, concentrated seawater pumping flow regulating valves, water supplementing flow regulating valves and connecting pipelines which are connected in series, wherein each falling film evaporator is composed of an evaporator, a spraying device, a fresh water slot, a demister, a water distributing pump and a seawater preheater; a steam circulating compressor is arranged between the evaporator in the last stage and a heating chamber in the first stage; waste heat exchange devices are respectively arranged on the pipelines used for discharging concentrated seawater and fresh water; and seawater firstly flows through the fresh water waste heat exchange device and the concentrated seawater waste heat exchange device, then enter the seawater preheater of the evaporator in the next-to-last stage, and then sequentially flows through the seawater preheaters in the previous stages and finally enters the evaporator in the first stage by virtue of the water supplementing flow regulating valve of the evaporator in the first stage. The multistage vacuum distillation seawater desalting device provided by the utility model has the advantages that a cooling device is eliminated, temperature difference between the discharged concentrated seawater and fresh water and the fresh seawater is small, and heat efficiency is higher.

Description

A kind of multilevel vacuum distilling sea water desalinating plant
(1) technical field
The utility model relates to a kind of multilevel vacuum distilling sea water desalinating plant, is mainly used in seawater and brackish water desalination.Belong to field of sea water desalting technology.
(2) background technology
The method that seawater and brackish water are desalinated is a lot, and conventional method has distillation method, reverse osmosis membrane and cold method etc.Widely used method mainly contains multistage flash evaporation (MSF) sea water desalinating plant and multi-effect distilling (MED) sea water desalinating plant in distillation method.
For the effect distillation seawater desalinating device of multi in the distillation method, water generation ratio is the important factor that affects the effect distillation seawater desalinating device of multi water producing cost.The water generation ratio of existing effect distillation seawater desalinating device of multi generally only has about 10-15, and the steam cost of at present effect distillation seawater desalinating device of multi use has reached 150 yuan/tons, and the steam cost of producing fresh water consumption per ton is at least 10 yuan/tons.The too high serious application that restricts the multiple-effect distillation sea water desalting technology of energy cost.
" the Novel multi-effect distillation seawater desalinating device " that patent ZL200920293053.1 and patent ZL200920270259.2 provide and " multilevel vacuum distilling sea water desalinating plant ", existing multiple-effect distillation sea water desalting technology is improved, although water generation ratio is significantly improved, but the steam cost of desalination water per ton still reaches more than 6 yuan/tons, the total cost of fresh water per ton has still surpassed 8 yuan/tons, and this still is unacceptable for existing 2-3 yuan/ton Urban water supply cost.
In the analysis to the factor of multiple-effect distillation sea water desalting technique influence water generation ratio, I find that the principal element that affect water generation ratio has three: one is employing vapour compression technology (TVC or MVC).One is concentration ratio, and concentration ratio is higher, and water generation ratio is higher.Another one is the temperature difference of discharging finished product fresh water and concentrated seawater and fresh seawater, and the temperature difference is less, and water generation ratio is higher.
Although above-mentioned two patents have improved concentration ratio, but the temperature of discharging concentrated seawater and finished product fresh water is still very high, with 25 ℃ of temperature heads that still have 15 ℃ of seawater temperature design load, and during winter operation the temperature difference up to more than 30 ℃, therefore be necessary further to reduce the temperature difference, improve water generation ratio.
(3) summary of the invention
In order to overcome the shortcoming of above-mentioned effect distillation seawater desalinating device of multi, the utility model provides a kind of the steam cycle compressor has been housed, and the multilevel vacuum distilling sea water desalinating plant of finished product fresh water heat recovery heat exchanger and concentrated seawater heat recovery heat exchanger.
The steam cycle compressor is transported to the whole heating cycle of steam that the last step vaporizer produces in the heating chamber of the first step, thereby has cancelled water cooler, and the steam iterative cycles of last step utilizes; Waste heat recovery has improved the temperature of fresh seawater, reduced the temperature head of finished product fresh water and concentrated seawater and fresh seawater, so thermo-efficiency is higher.
The present utility model realizes by following dual mode:
First kind of way:
A kind of multilevel vacuum distilling sea water desalinating plant, falling-film evaporator, interstage flow variable valve, fresh water tank and vacuum extractor, pump drainage concentrated seawater pump, pump drainage fresh water pump, fresh seawater transferpump by some grades of series connection, connecting pipeline between pump drainage concentrated seawater flow control valve, first step refill flow variable valve and double effect evaporator forms, and every one-level falling-film evaporator is comprised of vaporizer, spray equipment, fresh-water tank, scum dredger, cloth water pump, seawater preheating device.A steam cycle compressor in the end is housed between the heating chamber of the evaporator room of one-level vaporizer and first evaporator, at the pipeline of discharging concentrated seawater the concentrated seawater heat recovery heat exchanger of a series connection is housed, at the pipeline of discharging product fresh water the fresh water heat recovery heat exchanger of a series connection is housed.Fresh seawater is fresh water heat recovery heat exchanger and the concentrated seawater heat recovery heat exchanger by connecting at first, then enter the seawater preheating device of penultimate stage vaporizer, successively by the seawater preheating device of previous stage, enter at last the vaporizer of the first step by the refill flow variable valve of first evaporator again.
The second way:
A kind of multilevel vacuum distilling sea water desalinating plant, be comprised of the connecting pipeline between floodedevaporator, interstage flow variable valve, fresh water tank and vacuum extractor, pump drainage concentrated seawater pump, pump drainage fresh water pump, fresh seawater transferpump, pump drainage concentrated seawater flow control valve, first step refill flow variable valve and the double effect evaporator of some grades of series connection, every one-level floodedevaporator is comprised of vaporizer, fresh-water tank, scum dredger, seawater preheating device.A steam cycle compressor in the end is housed between the heating chamber of the evaporator room of one-level vaporizer and first evaporator, the pipeline of discharging concentrated seawater be equipped with a series connection the concentrated seawater heat recovery heat exchanger, at the pipeline of discharging product fresh water the fresh water heat recovery heat exchanger of a series connection is housed.Fresh seawater is at first by fresh water heat recovery heat exchanger and concentrated seawater heat recovery heat exchanger in parallel, then enter the seawater preheating device of penultimate stage vaporizer, successively by the seawater preheating device of previous stage, enter at last the vaporizer of the first step by the refill flow variable valve of first evaporator again.
Described steam cycle compressor is comprised of the mechanical vapor compressor of well heater and a series connection.
Described steam cycle compressor is comprised of well heater and two mechanical vapor compressors that are installed in series in the well heater both sides.
Described steam cycle compressor is comprised of mechanical vapor compressor.
A flow control valve all is housed on the fresh water line between the described adjacent double effect evaporator.
(4) description of drawings
Fig. 1 is an embodiment of the present utility model.
Fig. 2 is another one embodiment of the present utility model.
Among Fig. 1: the 1st, first step refill flow variable valve, the 2nd, the fresh-water tank of the first step, the 3rd, the heating chamber of first evaporator, the 4th, the falling-film evaporator of the first step, the 5th, spray equipment, the 6th, the seawater preheating device of the first step, the 7th, cloth water pump, the 8th, the heating chamber of the second stage, 9 is two inter-stage flow control valves, the 10th, and the fresh-water tank of the second stage, the 11st, well heater, the 12nd, the steam cycle compressor, 13 mechanical vapor compressors, the seawater preheating device of 14 penultimate stage vaporizers, the 15th, the fresh-water tank of last step, the 16th, the evaporator room of last step vaporizer, the 17th, the concentrated seawater groove of last step, the 18th, pump drainage concentrated seawater flow control valve, the 19th, concentrated seawater heat recovery heat exchanger, the 20th, pump drainage concentrated seawater pump, the 21st, fresh water heat recovery heat exchanger, the 22nd, fresh seawater transferpump, the 23rd, pump drainage fresh water pump, the 24th, fresh water tank and vacuum extractor, the 25th, the fresh water line flow control valve between the front and back stages vaporizer fresh-water tank.
Among Fig. 2: the 1st, first step refill flow variable valve, the 2nd, the heating chamber of first evaporator, the 3rd, first step floodedevaporator, the 4th, the fresh-water tank of the first step, 5 first step are scum dredgers, the 6th, and the seawater preheating device of the first step, the 7th, the flow control valve between the first step and the second stage, the 8th, mechanical vapor compressor, the 9th, steam cycle compressor, the 10th, well heater, the 11st, the seawater preheating device of penultimate stage vaporizer, the 12nd, the evaporator room of rear one-level vaporizer, the 13rd, pump drainage concentrated seawater flow control valve, the 14th, pump drainage concentrated seawater pump, the 15th, fresh water tank and vacuum extractor, the 16th, the pump drainage fresh water pump, the 17th, concentrated seawater heat recovery heat exchanger, the 18th, fresh water heat recovery heat exchanger, the 19th, fresh seawater transferpump, the 20th, the fresh-water tank of last step vaporizer, the 21st, the fresh water line flow control valve between the double effect evaporator fresh-water tank.
(5) embodiment
Fig. 1 is based on an embodiment of effect distillation seawater desalinating device of multi.
Heating steam enters the heating chamber (3) of first evaporator by the A mouth, and the vapor condenses of input discharges the heat of condensation, and the fresh water that condenses flows in the fresh-water tank (2); The seawater cloth water pump (7) of the first step is sent to spray equipment (5) to the seawater of first evaporator bottom, and spray equipment (5) forms falling liquid film on the surface of the prolong (4) of the first step, and falling liquid film is heated by the heat of condensation and seethes with excitement; The secondary steam that the first evaporator boiling produces at first passes through scum dredger, the steam that filters out seawater enters the seawater preheating device (6) of the first step, part vapor condenses heating seawater, most steam enters in the heating chamber (8) of the second stage, the moisture film of prolong outside, the second stage discharges the heat of condensation by the secondary steam condensation, the seawater of prolong outside, the second stage is heated boiling, the steam that the second stage produces at first passes through scum dredger, then enter in the seawater preheating device of the second stage, enter again in the heating chamber of third evaporator, produce steam with this to the last one-level vaporizer boiling that circulates.
The fresh water that condenses that the second stage produces flows in the fresh-water tank (10) of the second stage, fresh water in the first step fresh-water tank (2) passes through fresh water line, enter under suction function in the fresh-water tank (10) of the second stage, the fresh water that the fresh water after the flash distillation produces with second stage vaporizer enters the fresh-water tank of the 3rd utmost point.By that analogy, the fresh water that condenses of previous stages all flow in the fresh-water tank (15) of last step by the fresh water line of each inter-stage successively.
Enter the vaporizer of the first step through the refill flow variable valve (1) of the heated fresh seawater of one group of seawater preheating device (from 14 to 6) by the first step, the seawater of first evaporator bottom enters under suction function in the vaporizer of the second stage by two inter-stage flow control valves (9), can keep the sea level fluctuations of vaporizers at different levels to be stabilized in design water level by controlling refill flow variable valve at different levels.The last step vaporizer has a pump drainage concentrated seawater flow control valve (18), can control the concentration of discharging concentrated seawater by controlling this variable valve.
The secondary steam that vaporizers at different levels produce enters the next stage vaporizer successively, until the boiling of last step vaporizer.The steam that the last step vaporizer produces is heated, boosts by the steam cycle compressor (12) that is comprised of mechanical vapor compressor (13) and well heater (11), and the steam in the last step evaporator evaporation chamber (16) all is transported to the interior secondary use of heating chamber (3) of first evaporator by steam cycle compressor (12).Heating steam enters well heater (11) from the B mouth, and water of condensation and unnecessary steam are discharged from the C mouth.
Above-mentioned steam cycle compressor (12) forms by well heater (11) with a mechanical vapor compressor that is installed in series (13).
Mechanical vapor compressor (13) can be installed in series in the front of well heater (11), also can be installed in series in the back of well heater (11).The steam cycle compressor also can be comprised of well heater (11) and two mechanical vapor compressors that are installed in series in the well heater both sides.Steam cycle compressor (12) also can be comprised of one or more series connection or mechanical vapor compressor in parallel separately.
In the sea water desalinating plant operational process, to regulate in real time the quantity of steam that enters the A mouth and enter well heater (11) B mouth, guarantee that the steam that the last step vaporizer produces can all be transported in the heating chamber (3) of first evaporator by steam cycle compressor (12), can close the A mouth when quantity of steam is excessive.
The fresh water that last step condenses flows in the fresh-water tank (15) of last step, and the fresh water that condenses of previous stages also all flow in the fresh-water tank (15) of last step by the fresh water line of each inter-stage successively, the D mouth is connecting vacuum pump, the vacuum that vacuum pump produces by fresh water tank (24), the fresh water of last step is extracted in the fresh water tank (24), also the incondensable gas in the vaporizers at different levels is extracted out simultaneously.
A flow control valve (25) is arranged on the fresh water line between the adjacent double effect evaporator, be used for regulating the speed of taking out fresh water and taking out noncondensing gas.
Fresh seawater is sent in the tube side of product fresh water heat recovery heat exchanger (21) by the G mouth by fresh seawater transferpump (22), pump drainage fresh water pump (23) is extracted product fresh water out in fresh water tank (24), and send in the shell side of product fresh water heat recovery heat exchanger (21), fresh seawater is heated by product fresh water, product fresh water temperature decreases, and discharges from the F mouth.
By the fresh seawater of product fresh water heat recovery heat exchanger (21) heating, enter by pipeline in the tube side of concentrated seawater heat recovery heat exchanger (19), pump drainage concentrated seawater pump (20) is extracted the concentrated seawater in the last step vaporizer out by pump drainage concentrated seawater flow control valve (18), send in the shell side of concentrated seawater heat recovery heat exchanger (19), fresh seawater by product fresh water heat recovery heat exchanger (21) heating is heated by concentrated seawater again, and the concentrated seawater after the heat exchange is discharged from the E mouth.
Consider the possibility of seawater fouling in interchanger, convenient for scale removal, fresh seawater is walked the tube side of product fresh water heat recovery heat exchanger (21) and is advisable.Fresh seawater is walked shell side in concentrated seawater heat recovery heat exchanger (19), and concentrated seawater is walked tube side and is advisable.And concentrated seawater heat recovery heat exchanger (19) and product fresh water heat recovery heat exchanger (21) can exchange front and back position mutually.
By the fresh seawater of product fresh water heat recovery heat exchanger (21) and concentrated seawater heat recovery heat exchanger (19) preheating, the interior continuation of seawater preheating device (14) that at first is admitted to the penultimate stage vaporizer heated, then enter successively the seawater preheating device of previous stage, the seawater preheating device (6) from the first step enters the vaporizer of the first step by first step refill flow variable valve (1) at last.
Fig. 2 is based on an embodiment of vertical tube immersion multilevel vacuum distilling sea water desalinating plant.
Heating steam enters the heating chamber (2) of first evaporator by the A mouth, and the vapor condenses of input discharges the heat of condensation, and the seawater in the evaporator condensation pipe is heated evaporation, and the fresh water that condenses flows in the fresh-water tank (4).The secondary steam that the first evaporator boiling produces is at first by scum dredger (5), the steam that filters out seawater enters the seawater preheating device (6) of the first step, part vapor condenses heating seawater, most steam enters in the heating chamber of the second stage, the secondary steam condensation of prolong outside, the second stage discharges the heat of condensation, seawater in the prolong is heated boiling, the steam that the second stage produces passes through scum dredger equally, enter again in the seawater preheating device of the second stage, then enter in the heating chamber of third evaporator, with this to the last one-level vaporizer boiling that circulates.
Fresh water in the first step fresh-water tank (4) passes through fresh water line, under suction function, enter in the fresh-water tank of the second stage, the fresh water that fresh water after the flash distillation produces with second stage vaporizer enters the fresh-water tank of the 3rd utmost point, all enters in the fresh-water tank (20) of last step vaporizer at last.A fresh water line flow control valve (21) is arranged between the front and back stages fresh-water tank, and flow control valve is used for regulating the speed of taking out fresh water and taking out incondensable gas.
Enter the vaporizer of the first step through the refill flow variable valve (1) of the heated fresh seawater of one group of seawater preheating device (from 11 to 6) by the first step, seawater in the first evaporator enters under suction function in the vaporizer of the second stage by two inter-stage flow control valves (7), can keep the sea level fluctuations of vaporizers at different levels to be stabilized in design water level by controlling flow control valve at different levels.The last step vaporizer has one to be pump drainage concentrated seawater flow control valve (13), can control the concentration of discharging concentrated seawater by controlling this variable valve.
The secondary steam that vaporizers at different levels produce enters the next stage vaporizer successively, until the boiling of last step vaporizer.The steam that the last step vaporizer produces is heated, boosts by the steam cycle compressor (9) that is comprised of mechanical vapor compressor (8) and well heater (10), and the steam in the last step evaporator evaporation chamber (12) all is transported to the interior secondary use of heating chamber (2) of first evaporator by steam cycle compressor (9).Heating steam enters well heater (10) from the B mouth, and water of condensation and unnecessary steam are discharged from the C mouth.
Above-mentioned steam cycle compressor (9) forms by well heater (10) with a mechanical vapor compressor that is installed in series (8).
Mechanical vapor compressor (8) can be installed in series in the front of well heater (10), also can be installed in series in the back of well heater (10).Steam cycle compressor (9) also can be comprised of well heater (10) and two mechanical vapor compressors that are installed in series in well heater (10) both sides; Steam cycle compressor (9) also can be comprised of one or more series connection or mechanical vapor compressor in parallel separately.
In the sea water desalinating plant operational process, to regulate in real time the quantity of steam that enters the A mouth and enter well heater (10) B mouth, guarantee that the secondary steam that the last step vaporizer produces can all be transported in the heating chamber (2) of first evaporator by steam cycle compressor (9), can close the A mouth when quantity of steam is excessive.
The fresh water that the last step vaporizer condenses flows in the fresh-water tank (20) of last step, and the fresh water that condenses of previous stages vaporizer also all flow in the fresh-water tank (20) of last step by the fresh water line of each inter-stage successively, the D mouth is connecting vacuum pump, vacuum pump is extracted into the fresh water in the last step fresh-water tank (20) in the fresh water tank (15) by the vacuum that fresh water tank (15) produces, and also the incondensable gas in the vaporizers at different levels is extracted out simultaneously.
A flow control valve (21) is arranged on the fresh water line between the adjacent double effect evaporator, be used for regulating the speed of taking out fresh water and taking out noncondensing gas.
Fresh seawater, is sent into fresh seawater in the tube side of product fresh water heat recovery heat exchanger (18) in parallel and concentrated seawater heat recovery heat exchanger (17) by fresh seawater transferpump (19) simultaneously by the G mouth.Pump drainage concentrated seawater pump (14) is extracted the concentrated seawater in the last step vaporizer out by pump drainage concentrated seawater flow control valve (13), send in the shell side of concentrated seawater heat recovery heat exchanger (17), fresh seawater is heated by concentrated seawater, and the concentrated seawater after the heat exchange is discharged from the E mouth.Pump drainage fresh water pump (16) is extracted product fresh water out in fresh water tank (15), and sends in the shell side of product fresh water heat recovery heat exchanger (18), and fresh seawater is heated by product fresh water, and product fresh water temperature decreases, and discharges from the F mouth.
By the fresh seawater of product fresh water heat recovery heat exchanger (18) and concentrated seawater heat recovery heat exchanger (17) preheating, at first be admitted to again heating in the seawater preheating device (11) of penultimate stage vaporizer, then enter successively the seawater preheating device of previous stage, at last from the seawater preheating device (6) of the first step by being that first step refill flow variable valve (1) enters the vaporizer of the first step.
By the seawater flow regulating valve (7) between the control double effect evaporator, can control the height of every one-level vaporizer maritime interior waters, when vaporizer maritime interior waters water level was controlled at suitable height, the vaporizers at different levels in the present embodiment were exactly a standpipe climbing-film evaporator.

Claims (6)

1. a multilevel vacuum distilling sea water desalinating plant is comprised of the connecting pipeline between falling-film evaporator, interstage flow variable valve (9), fresh water tank and vacuum extractor (24), pump drainage concentrated seawater pump (20), pump drainage fresh water pump (23), fresh seawater transferpump (22), pump drainage concentrated seawater flow control valve (18), first step refill flow variable valve (1) and the double effect evaporator of some grades of series connection; Every one-level falling-film evaporator is comprised of vaporizer (4), spray equipment (5), fresh-water tank (2), scum dredger, cloth water pump (7), seawater preheating device (6), it is characterized in that: in the end between the heating chamber (3) of the evaporator room of one-level vaporizer (16) and first evaporator a steam cycle compressor (12) is housed; At the pipeline of discharging concentrated seawater the concentrated seawater heat recovery heat exchanger (19) of a series connection is housed, at the pipeline of discharging product fresh water the fresh water heat recovery heat exchanger (21) of a series connection is housed; Fresh seawater is at first by fresh water heat recovery heat exchanger (21) and concentrated seawater heat recovery heat exchanger (19), then enter the seawater preheating device (14) of penultimate stage vaporizer, enter successively the seawater preheating device of previous stage, the refill flow variable valve (1) by first evaporator enters the vaporizer of the first step at last again.
2. a multilevel vacuum distilling sea water desalinating plant is comprised of the connecting pipeline between floodedevaporator, interstage flow variable valve (7), fresh water tank and vacuum extractor (15), pump drainage concentrated seawater pump (14), pump drainage fresh water pump (16), fresh seawater transferpump (19), pump drainage concentrated seawater flow control valve (13), first step refill flow variable valve (1) and the double effect evaporator of some grades of series connection; Every one-level floodedevaporator is comprised of vaporizer (3), fresh-water tank (4), scum dredger (5), seawater preheating device (6), it is characterized in that: in the end between the heating chamber (2) of the evaporator room of one-level vaporizer (12) and first evaporator a steam cycle compressor (9) is housed; At the pipeline of discharging concentrated seawater the concentrated seawater heat recovery heat exchanger (17) of a series connection is housed, at the pipeline of discharging product fresh water the fresh water heat recovery heat exchanger (18) of a series connection is housed; Fresh seawater is at first by fresh water heat recovery heat exchanger (18) and concentrated seawater heat recovery heat exchanger (17), then enter the seawater preheating device (11) of penultimate stage vaporizer, enter successively the seawater preheating device of previous stage, the refill flow variable valve (1) by first evaporator enters the vaporizer of the first step at last again.
3. a kind of multilevel vacuum distilling sea water desalinating plant according to claim 1 and 2, it is characterized in that: the steam cycle compressor is comprised of the mechanical vapor compressor of well heater and a series connection.
4. a kind of multilevel vacuum distilling sea water desalinating plant according to claim 1 and 2 is characterized in that: the steam cycle compressor is comprised of well heater and two mechanical vapor compressors being installed in series in the well heater both sides.
5. a kind of multilevel vacuum distilling sea water desalinating plant according to claim 1 and 2, it is characterized in that: the steam cycle compressor is comprised of mechanical vapor compressor.
6. a kind of multilevel vacuum distilling sea water desalinating plant according to claim 1 and 2 is characterized in that: a flow control valve all is housed on the fresh water line between the adjacent double effect evaporator.
CN2012200687208U 2012-02-29 2012-02-29 Multistage vacuum distillation seawater desalting device Active CN202849193U (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2648323C1 (en) * 2017-06-06 2018-03-23 федеральное государственное автономное образовательное учреждение высшего образования "Самарский национальный исследовательский университет имени академика С.П. Королёва" Method of operation of a steam compressor of a multistage particular mounting unit and device for its implementation
CN108006608A (en) * 2017-11-22 2018-05-08 山东伯仲真空设备股份有限公司 Afterheat of hot water recoverying and utilizing method

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2648323C1 (en) * 2017-06-06 2018-03-23 федеральное государственное автономное образовательное учреждение высшего образования "Самарский национальный исследовательский университет имени академика С.П. Королёва" Method of operation of a steam compressor of a multistage particular mounting unit and device for its implementation
CN108006608A (en) * 2017-11-22 2018-05-08 山东伯仲真空设备股份有限公司 Afterheat of hot water recoverying and utilizing method

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