CN106587238A - Sea water desalination system and method with low temperature exhaust heat utilization function - Google Patents
Sea water desalination system and method with low temperature exhaust heat utilization function Download PDFInfo
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- CN106587238A CN106587238A CN201710051550.XA CN201710051550A CN106587238A CN 106587238 A CN106587238 A CN 106587238A CN 201710051550 A CN201710051550 A CN 201710051550A CN 106587238 A CN106587238 A CN 106587238A
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- 239000013535 sea water Substances 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 43
- 238000010612 desalination reaction Methods 0.000 title claims abstract description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 93
- 238000011084 recovery Methods 0.000 claims abstract description 9
- 239000006200 vaporizer Substances 0.000 claims description 39
- 238000007654 immersion Methods 0.000 claims description 32
- 230000000694 effects Effects 0.000 claims description 27
- 239000012530 fluid Substances 0.000 claims description 20
- 239000012267 brine Substances 0.000 claims description 18
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 18
- 239000000047 product Substances 0.000 claims description 14
- 238000011033 desalting Methods 0.000 claims description 13
- 239000000463 material Substances 0.000 claims description 12
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims description 9
- 239000002826 coolant Substances 0.000 claims description 8
- 239000013589 supplement Substances 0.000 claims description 7
- 238000009833 condensation Methods 0.000 claims description 6
- 230000005494 condensation Effects 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 6
- 230000008569 process Effects 0.000 abstract description 11
- 238000004821 distillation Methods 0.000 abstract description 10
- 239000013505 freshwater Substances 0.000 abstract description 8
- 238000011109 contamination Methods 0.000 abstract 1
- 238000001704 evaporation Methods 0.000 description 11
- 230000008020 evaporation Effects 0.000 description 9
- 239000000126 substance Substances 0.000 description 9
- 239000012153 distilled water Substances 0.000 description 8
- 238000012423 maintenance Methods 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 7
- 230000005611 electricity Effects 0.000 description 4
- 238000007701 flash-distillation Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000008439 repair process Effects 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 238000005482 strain hardening Methods 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 206010000372 Accident at work Diseases 0.000 description 1
- 241000628997 Flos Species 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000003115 biocidal effect Effects 0.000 description 1
- 239000003139 biocide Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000013530 defoamer Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000000686 essence Substances 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000000452 restraining effect Effects 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention provides a sea water desalination system and method with a low temperature exhaust heat utilization function, and particularly provides a multiple-effect distillation sea water desalination system and method suitable for utilization of low temperature exhaust heat of a refinery enterprise. The sea water desalination system comprises an immersed vapor generator 3 and an MED system. The problems that the refinery enterprise has difficulty in low temperature exhaust heat recovery and is low in exhaust heat recovery level, the purposes of saving energy, reducing emission and effectively reducing sea water desalination cost are achieved, and the problem that the coastal refinery enterprise has difficulty in fresh water utilization. The immersed vapor generator is arranged in the sea water desalination system with the low temperature exhaust heat utilization function, which is equivalent to integrating a dividing wall type heat exchanger and a flash chamber in a traditional scheme and integrating dividing wall type heat exchange and vapor generation, the sea water desalination system is suitable for the refinery enterprise to recover low-temperature process water contaminated possibly, the contamination risk of water produced through sea water desalination is greatly reduced, the system is simplified, operation control is easier, and less area is occupied.
Description
Technical field
The invention belongs to field of seawater desalination, more particularly, to a kind of low as thermal source with Petrochemical Enterprises low temperature process hot water
Warm UTILIZATION OF VESIDUAL HEAT IN seawater desalination system and method.
Background technology
Petrochemical Enterprises often have substantial amounts of low temperature exhaust heat, and (return water temperature is required as 70 DEG C mainly 95 DEG C of technique hot water
Left and right).At present, the heat utilization level of domestic refinery factory low temperature exhaust heat is very low, although in recent years by Introduced From Abroad low temperature exhaust heat
The technology of recycling, starts for low temperature exhaust heat to be used for the aspects such as warm heating, utilizing waste heat for refrigeration that generate electricity, tie up, but effect is less, and still
So there are many low temperature exhaust heats directly to be discharged, both caused the repetition and waste of the energy, and thermal pollution is generated to environment.
Solving in the middle of the nervous all multi-methods of freshwater resources, desalinization is a kind of practical and effective method,
Especially for coastal cities and island.But desalinization is energy-intensive industry, and adopting current desalinator more
Fossil fuel.The high energy consumption of desalinization causes water producing cost to remain high, and on the other hand, a large amount of fuel that burn are released in environment
Substantial amounts of greenhouse gases are released, and also very big pressure are brought to environment.How further to reduce the controlling the water circulation of sea water desalinating unit into
This has become international desalinization circle key issue to be solved.
In existing technology, low-temperature multiple-effect distillation sea water desalting system (abbreviation MED systems, similarly hereinafter) is needed with steam
As input thermal source, when external heat source is hot water, hot water is first transformed into steam and could supply the use of MED systems by needs.
On the premise of being not provided with additional heaters (electric heater, the gas/oil/coal heater of combustion etc.), the conventional of steam is produced using hot water
Method is flash method, will hot water import in a large space container, the container inner pressure is lower than heat hydraulic pressure, then hot water meeting
Generation flash distillation, produces a part of steam, and the temperature of steam is equal to the corresponding saturation temperature of container inner pressure, this some vapor conduct
The input thermal source of MED systems, i.e. " hot water flash evaporation+MED " technique.
(such as may be each containing process upstream flow process in the technique hot water of refinery when there is volatile material in thermal source hot water
The hydrocarbons that link is leaked out) when, the direct flash method of hot water of traditional method is no longer safe for MED systems, because
For chemical gas leak material may be contained in hot water, during the direct flash distillation of hot water, some drops, the chemical industry in drop in steam, can be carried secretly
Material can enter MED systems with steam, have very maximum probability polluted seawater desalination to produce water；Low-temperature water heating is utilized directly, in hot water
The oil product of leakage is too many, and direct flash distillation is also possible that the possibility of blast, reveals medium and brings safety in production hidden danger, will seriously send out
Raw industrial accident；In addition, directly utilizing low-temperature water heating, it is also possible to which desalting plant is adversely affected, such as pipeline is dirty stifled
And increase cleaning frequency etc..
In this regard, there is design to consider once to exchange heat chemical industry hot water using plate type heat exchanger, i.e., chemical industry hot water is made
The hot side runner of plate type heat exchanger is flow through for hot working fluid, pure distilled water flows through the cold side stream of plate type heat exchanger as cold working medium
Road, the heat of such chemical industry hot water are just transmitted and give distilled water, and this part distilled water is re-introduced in flash chamber with flash distillation
Go out steam to use for MED systems, i.e. " plate type heat exchanger+flash vessel+MED " technique.The program utilizes plate type heat exchanger blockingization
Work hot water and the directly contact of MED systems, serve intermediate heat transfer effect, greatly reduce the pollution wind of sea-water-desalination water producing
Danger.But, the program makes system become more complicated, increased operation control fussy degree, and additionally increase it is board-like
Heat exchanger causes system footprint and investment also corresponding increase.
The content of the invention
In view of this, it is contemplated that proposing that a kind of low temperature heat seawater desalination system and method, i.e. immersion steam
Vapour generator and low-temperature multiple-effect distillation sea water desalting coupled system and method for desalting seawater, it is multiple to solve existing system structure
It is miscellaneous, operation control it is loaded down with trivial details, and investment of occupation of land it is big the problems such as.
To reach above-mentioned purpose, the technical scheme is that what is be achieved in that：
A kind of low temperature heat seawater desalination system, including immersion steam generator 3 and MED systems；
The immersion steam generator 3 is provided with hot working fluid entrance, hot working fluid outlet, water supplement port and steam (vapor) outlet；
The steam (vapor) outlet is connected with the tube side of the 1st effect vaporizer of MED systems by jet chimney 8；
The steam condensate of the 1st effect vaporizer of the MED systems is connected with the water supplement port by condensing water conduit 9.
Further, the technique hot water water pipe of the hot working fluid entrance of the immersion steam generator 3 and refinery system
Road 10 is connected, and the hot working fluid outlet of the immersion steam generator 3 is connected with the technique hot water water return pipeline 11 of refinery system.
Further, shell-and-tube heat exchanger of the immersion steam generator 3 for carrying vapour room.
Further, the shell-and-tube heat exchanger include housing, the heat-exchanging tube bundle being arranged in housing and with the housing
Connected vaporium, the vaporium are provided with the steam (vapor) outlet, and the hot working fluid entrance, hot working fluid outlet are arranged on described
Heat-exchanging tube bundle two ends.
Further, the MED systems include sea water supply pipeline 14, condenser 2, low-temperature multi-effect vaporizer group 1 and sea
Water discharge spout road 15；
The sea water supply pipeline 14 is connected with the condenser 2, and 2 coolant outlet of the condenser is low with described respectively
Warm multi-effect evaporator group 1, seawater discharge pipeline 15 are connected；
The steam (vapor) outlet and latter effect of 1st effective evaporator before along steam flow direction, the low-temperature multi-effect vaporizer group 1
The steam inlet of vaporizer is connected, the steam (vapor) outlet and the condenser 2 of the last evaporator of the low-temperature multi-effect vaporizer group 1
Steam inlet be connected；
In the condensation-water drain and low-temperature multi-effect vaporizer group 1 of the condenser 2,2nd effect evaporator is to last evaporator
Steam condensation water out be respectively connected with product water recovery tube 13；
Strong brine connection strong brine discharge tube 12 in low-temperature multi-effect vaporizer group 1.
Further, the strong brine discharge tube 12 is provided with strong brine emptying pump 5；
The product water recovery tube 13 is provided with product water pump 4；
The coolant outlet of the condenser 2 passes through material sea water booster pump 7 and 1 phase of low-temperature multi-effect vaporizer group
Even.
Further, 2 coolant outlet of the condenser passes through material sea water booster pump 7 and spray equipment is uniformly sprayed and arrived
In the low-temperature multi-effect vaporizer group 1 outside the heat-exchanging tube bundle of each effect vaporizer.
Further, the condensing water conduit 9 is provided with condensate pump 6.
The present invention also provides a kind of method for desalting seawater, carries out desalinization, immersion steam generator using MED systems
(3) produce steam thermal source is provided for MED systems.
Relative to prior art, low temperature heat seawater desalination system of the present invention has the advantage that：
In low temperature heat seawater desalination system of the present invention, the setting of immersion steam generator is equivalent to knot
The dividing wall type heat exchanger and flash chamber in traditional scheme is closed, has been integrated intermediate heat transfer and steam generating function, was both dropped significantly
Low sea-water-desalination water producing pollution risk, in turn simplify system, make that operation manipulation is simpler, and occupation of land is more saved；
Can multiple stage in parallel, realize online switching and on-bne repair, meet the design requirement of petrochemical industry Refining Chemical Industry, i.e.,
Make upstream that leakage to occur, even if can also realize cut-out and handoff functionality, both no potential safety hazard, was just nor affecting on desalting plant
Often run；
The present invention carries out the process route of low temperature multiple-effect distillation sea water desalting, not only using the low temperature exhaust heat of Petrochemical Enterprises
Energy-saving and emission-reduction can be reached, the purpose of desalinization cost is effectively reduced, and it is difficult to solve coastal Petrochemical Enterprises water
Problem.
Description of the drawings
The accompanying drawing for constituting the part of the present invention is used for providing a further understanding of the present invention, the schematic reality of the present invention
Apply example and its illustrate, for explaining the present invention, not constituting inappropriate limitation of the present invention.In the accompanying drawings：
Fig. 1 is the structural representation of low temperature heat seawater desalination system of the present invention.
1- low-temperature multi-effect vaporizer groups；2- condensers；3- immersion steam generators；4- water pumps；5- strong brine emptying pumps；
6- condensate pumps；7- material sea water booster pumps；8- jet chimneys；9- condensing water conduits；The technique hot water water of 10- refinery systems
Pipeline；The technique hot water water return pipeline of 11- refinery systems；12- strong brine discharge tubes；13- product water recovery tubes；14- sea water
Service；15- seawater discharge pipelines.
Specific embodiment
It should be noted that in the case where not conflicting, the embodiment and the feature in embodiment in the present invention can phase
Mutually combine.
In describing the invention, it is to be understood that term " " center ", " longitudinal direction ", " horizontal ", " on ", D score,
The orientation or position relationship of the instruction such as "front", "rear", "left", "right", " vertical ", " level ", " top ", " bottom ", " interior ", " outward " is
Based on orientation shown in the drawings or position relationship, it is for only for ease of the description present invention and simplifies description, rather than indicate or dark
Show that the device or element of indication there must be specific orientation, with specific azimuth configuration and operation therefore it is not intended that right
The restriction of the present invention.Additionally, term " first ", " second " etc. are only used for describing purpose, and it is not intended that indicating or implying phase
To importance or the implicit quantity for indicating indicated technical characteristic.Thus, the feature for defining " first ", " second " etc. can
To express or implicitly include one or more this feature.In describing the invention, unless otherwise stated, " multiple "
It is meant that two or more.
In describing the invention, it should be noted that unless otherwise clearly defined and limited, term " installation ", " phase
Company ", " connection " should be interpreted broadly, for example, it may be being fixedly connected, or being detachably connected, or be integrally connected；Can
Being to be mechanically connected, or electrically connect；Can be joined directly together, it is also possible to be indirectly connected to by intermediary, Ke Yishi
The connection of two element internals.For the ordinary skill in the art, above-mentioned term can be understood by concrete condition
Concrete meaning in the present invention.
Below with reference to the accompanying drawings and in conjunction with the embodiments describing the present invention in detail.
The present invention provides a kind of low temperature heat seawater desalination system, as shown in figure 1, including immersion steam generator
3 and MED systems；
Immersion steam generator 3 is provided with hot working fluid entrance, hot working fluid outlet, water supplement port and steam (vapor) outlet；
Steam (vapor) outlet is connected with the tube side of the 1st effect vaporizer of MED systems by jet chimney 8；
The steam condensate of the 1st effect vaporizer of MED systems is connected with water supplement port by condensing water conduit 9.
The hot working fluid entrance of immersion steam generator 3 is connected with the technique hot water water pipeline 10 of refinery system, submergence
The hot working fluid outlet of formula steam generator 3 is connected with the technique hot water water return pipeline 11 of refinery system.
Shell-and-tube heat exchanger of the immersion steam generator 3 for carrying vapour room.
The vaporium that shell-and-tube heat exchanger is included housing, the heat-exchanging tube bundle being arranged in housing and is connected with housing, steam
Room is provided with steam (vapor) outlet, and hot working fluid entrance, hot working fluid outlet are arranged on heat-exchanging tube bundle two ends.
MED systems include sea water supply pipeline 14, condenser 2, low-temperature multi-effect vaporizer group 1 and seawater discharge pipeline 15；
Sea water supply pipeline 14 is connected with condenser 2,2 coolant outlet of condenser respectively with low-temperature multi-effect vaporizer group 1,
Seawater discharge pipeline 15 is connected；
The steam (vapor) outlet of 1st effective evaporator and latter effect evaporation before along steam flow direction, low-temperature multi-effect vaporizer group 1
The steam inlet of device is connected, the steam (vapor) outlet of the last evaporator of low-temperature multi-effect vaporizer group 1 and the steam inlet phase of condenser 2
Even；
The steaming of 2nd effect evaporator to last evaporator in the condensation-water drain and low-temperature multi-effect vaporizer group 1 of condenser 2
Vapour condenses water out and is respectively connected with product water recovery tube 13；
Strong brine connection strong brine discharge tube 12 in low-temperature multi-effect vaporizer group 1.
Strong brine discharge tube 12 is provided with strong brine emptying pump 5；
Product water recovery tube 13 is provided with product water pump 4；
The coolant outlet of condenser 2 is connected with low-temperature multi-effect vaporizer group 1 by material sea water booster pump 7.
2 coolant outlet of condenser passes through material sea water booster pump 7 and spray equipment uniformly sprays low-temperature multi-effect and evaporates
In device group 1 outside the heat-exchanging tube bundle of each effect vaporizer.
Condensing water conduit 9 is provided with condensate pump 6.
The course of work of this example：Refinery technique hot water is sent out into immersion steam by refinery technique hot water water pipeline 10
Raw device 3, refinery technique hot water are walked tube side, are flow through from heat exchanger tube beam tube, then flow out from hot working fluid outlet, and by refinery technique
Hot water backwater's pipeline 11 is discharged.Pure distilled water is entered the shell side of immersion steam generator 3 as cold working medium by water supplement port,
In enclosure interior, heat-exchanging tube bundle is immersed in distilled water, and distilled water is by the refinery technique hot water heating inside heat-exchanging tube bundle and steams
Send out, steam is converged in steam room.
Steam in 3 steam room of immersion steam generator enters MED systems the 1st by jet chimney 8 and imitates vaporizer envelope
Head, it is internal subsequently into the 1st effect evaporator heat exchange tube bank, by the sea water cooling outside tube bank, distilled water is condensed into, the 1st is imported
Effect vaporizer freshwater room, is finally returned in 3 housing of immersion steam generator by condensing water conduit 9.
Sea water Jing sea water supplies pipeline 14 enters condenser 2, is that last evaporator is produced by MED systems last 1st effective evaporator
Raw steam condensation, own temperature are raised, and a part uniformly sprays MED systems as the material water Jing spray equipments of MED systems
Outside the heat-exchanging tube bundle of each effect vaporizer of system, remaining sea water then flows back to sea through seawater discharge pipeline 15；In the 1st effect evaporation
In device, the steam that immersion steam generator 3 is produced enters into the 1st effect evaporator heat exchange tube bank inside the condensation in restraining,
The heat for being discharged causes the sea water part sprayed in tube bank to evaporate, produced steam into the 2nd effect vaporizer, the
Condensing in the tube bank of 2 effect vaporizers, and discharge heat causes the sea water part sprayed in tube bank to evaporate, produced steam
Vaporizer is imitated into the 3rd, by that analogy.The evaporating temperature of 1st effective evaporator is all the time than the evaporating temperature of front 1st effective evaporator afterwards
It is low.Material water all only some evaporations outside each effect heat exchange pipe of evaporator are sprayed, remaining part is (now referred to as dense
Saline) then stream arrives the bottom of vaporizer under gravity.Produced steam is flowed in the tube bank of latter effect, and continues generation
Condensation, condensing the distilled water that obtains becomes the product water of desalinization, and product water and strong brine are being flowed into from stream mode step by step
Next effect, to simplify structure and make full use of heat.Product water converges in condenser condensed water outlet and is taken out by product water pump 4
Go out, Jing fresh water pipeline 13 delivers to fresh-water tank.Strong brine is in the last 1st effective evaporator strong brine floss hole of MED systems by strong brine pump
5 discharge, and Jing strong brines discharge tube 5 flows back to sea.
Three kinds of " hot water flash evaporation+MED ", " plate type heat exchanger+flash vessel+MED " and " immersion steam generator+MED "
Technical scheme, process route basic simlarity in MED technological processes differ primarily in that front end thermal source Land use systems.
(1) " hot water flash evaporation ", " immersion steam generator " and " plate type heat exchanger+flash vessel " three kinds of steam generation modes
Table 1 below is referred in technical contrast：
Table 1
(2) by taking unit 15000t/d MED devices as an example, " hot water flash evaporation+MED ", " immersion steam generator+MED " and
" plate type heat exchanger+flash vessel+MED " three kinds of process route energy consumption comparisons are shown in Table 2：
For " hot water flash evaporation ", " immersion steam generator " and " plate type heat exchanger+flash vessel " three kinds of process routes, leaching
Do not have the system energy consumption of the process route of formula steam generator relatively low.
For separate unit 15000t/d MED, " hot water flash evaporation " power consumption more daily than " immersion steam generator " will have more
7500kWh (according to 0.5 yuan/kWh of electricity price, i.e., 3750 yuan), then the operating cost of a year will have more about 1,370,000 yuan；
" plate type heat exchanger+flash vessel " power consumption more daily than " immersion steam generator " will have more 9750kWh (according to electricity
0.5 yuan/kWh of valency, i.e., 4875 yuan), then the operating cost of a year will have more about 1,780,000 yuan.
So, immersion steam generator+MED most energy-conservations, are also optimal process route.
In addition, immersion steam generator+MED systems are compared with Conventional cryogenic multi-effect sea water desalting system, water producing cost
Substantially reduce：The UTILIZATION OF VESIDUAL HEAT IN low temperature multiple-effect distillation sea water desalting device is made water cost and can be divided into following several parts：Change
Learn chemical consumption, heating power consumption, power consumption, labor wage, welfare and administration fee, maintenance cost, equipment depreciation expense etc..
The depreciable life of engineering, desalting plant utilization rate of equipment and installations was calculated with 95% in terms of 25 years, and its each several part expense is as follows：
1). chemical drugss consumption
Before raw water enters low temperature multiple-effect distillation device, antisludging agent, defoamer etc. must be added.In addition, to ensure device
It is normal to go on a long journey, should periodically add biocide.The every year cleaning of low temperature multiple-effect distillation device once, the consumption of abluent according to
Scaling degree is determined.The chemical drugss expense of fresh water per ton is total about 0.3 yuan.
2). heating power consumption
Low temperature multiple-effect distillation device is UTILIZATION OF VESIDUAL HEAT IN, therefore the heating power consumption of fresh water per ton is 0 yuan.
3). power consumption
The power consumption 1.2kWh of low temperature multiple-effect distillation desalting engineering water per ton, if electricity price is in terms of 0.50 yuan/kWh, low temperature
The ton hydroelectric power cost of multi-effect distilling desalination is 0.6 yuan.
4). salary appropriate to a special post welfare expenses
Sea water desalinating unit automaticity is very high, is not required to set special messenger's operation and maintenance.
5). depreciation of fixed assets expense
The depreciable life of fixed assets is 25 years, and salvage value of fixed assets is 4%, the depreciation of fixed assets expense of fresh water per ton
About 1.2 yuan.
6). overhaul and maintenance repair maintenance cost
The overhaul of this device and maintenance repair maintenance expense take the 1.5% of original value of fixed assets, the overhaul of desalination water per ton and
Maintenance maintenance cost is 0.48 yuan.
So, it is as follows that UTILIZATION OF VESIDUAL HEAT IN low temperature multiple-effect distillation sea water desalting device makes water cost：
Unit makes water cost：2.58 yuan/ton, water producing cost is substantially reduced.
Presently preferred embodiments of the present invention is the foregoing is only, not to limit the present invention, all essences in the present invention
Within god and principle, any modification, equivalent substitution and improvements made etc. should be included within the scope of the present invention.
Claims (9)
1. a kind of low temperature heat seawater desalination system, it is characterised in that：Including immersion steam generator (3) and MED systems
System；
The immersion steam generator (3) is provided with hot working fluid entrance, hot working fluid outlet, water supplement port and steam (vapor) outlet；
The steam (vapor) outlet is connected with the tube side of the 1st effect vaporizer of MED systems by jet chimney (8)；
The steam condensate of the 1st effect vaporizer of the MED systems is connected with the water supplement port by condensing water conduit (9).
2. low temperature heat seawater desalination system according to claim 1, it is characterised in that：The immersion steam is sent out
The hot working fluid entrance of raw device (3) is connected with technique hot water water pipeline (10) of refinery system, the immersion steam generator
(3) hot working fluid outlet is connected with technique hot water water return pipeline (11) of refinery system.
3. low temperature heat seawater desalination system according to claim 1, it is characterised in that：The immersion steam is sent out
Shell-and-tube heat exchanger of the raw device (3) for carrying vapour room.
4. low temperature heat seawater desalination system according to claim 3, it is characterised in that：The shell-and-tube heat exchanger
The vaporium being connected including housing, the heat-exchanging tube bundle being arranged in housing and with the housing, the vaporium are provided with described
Steam (vapor) outlet, the hot working fluid entrance, hot working fluid outlet are arranged on the heat-exchanging tube bundle two ends.
5. the low temperature heat seawater desalination system according to any one of claim 1-4, it is characterised in that：The MED
System includes sea water supply pipeline (14), condenser (2), low-temperature multi-effect vaporizer group (1) and seawater discharge pipeline (15)；
The sea water supply pipeline (14) is connected with the condenser (2), condenser (2) coolant outlet respectively with it is described
Low-temperature multi-effect vaporizer group (1), seawater discharge pipeline (15) are connected；
Before along steam flow direction, the low-temperature multi-effect vaporizer group (1), the steam (vapor) outlet of 1st effective evaporator is steamed with latter effect
The steam inlet for sending out device is connected, the steam (vapor) outlet and the condenser of the last evaporator of the low-temperature multi-effect vaporizer group (1)
(2) steam inlet is connected；
In the condensation-water drain and low-temperature multi-effect vaporizer group (1) of the condenser (2), 2nd effect evaporator is to last evaporator
Steam condensation water out be respectively connected with product water recovery tube (13)；
Strong brine connection strong brine discharge tube (12) in low-temperature multi-effect vaporizer group (1).
6. low temperature heat seawater desalination system according to claim 5, it is characterised in that：
The strong brine discharge tube (12) is provided with strong brine emptying pump (5)；
The product water recovery tube (13) is provided with product water pump (4)；
The coolant outlet of the condenser (2) passes through material sea water booster pump (7) and low-temperature multi-effect vaporizer group (1) phase
Even.
7. low temperature heat seawater desalination system according to claim 5, it is characterised in that：The condenser (2) is cold
But water out passes through material sea water booster pump (7) and spray equipment is uniformly sprayed Dao the low-temperature multi-effect vaporizer group (1) in respectively
Outside the heat-exchanging tube bundle of effect vaporizer.
8. claim 1-4 or the low temperature heat seawater desalination system described in any one of 6-7 it is characterized in that：The condensation
Waterpipe (9) is provided with condensate pump (6).
9. a kind of method for desalting seawater, it is characterised in that：Desalinization, immersion steam generator (3) are carried out using MED systems
Produce steam thermal source is provided for MED systems.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108190988A (en) * | 2017-12-29 | 2018-06-22 | 常州思宇知识产权运营有限公司 | A kind of heat-pipe type sea-water desalinating using fume afterheat |
| WO2022046136A1 (en) | 2020-08-28 | 2022-03-03 | Saudi Arabian Oil Company | Utilizing waste heat for thermal desalination |
| CN114349245A (en) * | 2021-12-08 | 2022-04-15 | 中国科学院工程热物理研究所 | Clean energy driven seawater desalination system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106082378A (en) * | 2016-08-19 | 2016-11-09 | 北京今大禹环境技术股份有限公司 | A kind of low temperature (1+n) effect distillation seawater desalination technique |
| CN106115825A (en) * | 2016-08-19 | 2016-11-16 | 北京今大禹环境技术股份有限公司 | A kind of low temperature multiple-effect distillation seawater desalination system |
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- 2017-01-19 CN CN201710051550.XA patent/CN106587238A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106082378A (en) * | 2016-08-19 | 2016-11-09 | 北京今大禹环境技术股份有限公司 | A kind of low temperature (1+n) effect distillation seawater desalination technique |
| CN106115825A (en) * | 2016-08-19 | 2016-11-16 | 北京今大禹环境技术股份有限公司 | A kind of low temperature multiple-effect distillation seawater desalination system |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108190988A (en) * | 2017-12-29 | 2018-06-22 | 常州思宇知识产权运营有限公司 | A kind of heat-pipe type sea-water desalinating using fume afterheat |
| WO2022046136A1 (en) | 2020-08-28 | 2022-03-03 | Saudi Arabian Oil Company | Utilizing waste heat for thermal desalination |
| CN114349245A (en) * | 2021-12-08 | 2022-04-15 | 中国科学院工程热物理研究所 | Clean energy driven seawater desalination system |
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Effective date of registration: 20211119 Address after: 643001 whole building, No. 150, Huangjueping Road, Wuxing Street, Ziliujing District, Zigong City, Sichuan Province Applicant after: DONGFANG BOILER GROUP Co.,Ltd. Address before: 300462 No. 1, Lingang Economic Zone, Binhai New Area, Tianjin Applicant before: ZHONGHE SEAWATER DESALINATION ENGINEERING Co.,Ltd. |
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