CN101687668A - Desalination apparatus and method of desalination - Google Patents

Desalination apparatus and method of desalination Download PDF

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Publication number
CN101687668A
CN101687668A CN200780053079A CN200780053079A CN101687668A CN 101687668 A CN101687668 A CN 101687668A CN 200780053079 A CN200780053079 A CN 200780053079A CN 200780053079 A CN200780053079 A CN 200780053079A CN 101687668 A CN101687668 A CN 101687668A
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CN
China
Prior art keywords
evaporating pot
water
evaporating
heat
group
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Granted
Application number
CN200780053079A
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Chinese (zh)
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CN101687668B (en
Inventor
奥斯曼·艾哈迈德·哈马德
平井光芳
五味克之
前川和人
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Sasakura Engineering Co Ltd
Water Re-Use Promotion Center
Saline Water Conversion Corp Saudi Arabia
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Sasakura Engineering Co Ltd
Water Re-Use Promotion Center
Saline Water Conversion Corp Saudi Arabia
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Publication of CN101687668A publication Critical patent/CN101687668A/en
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Publication of CN101687668B publication Critical patent/CN101687668B/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/04—Evaporators with horizontal tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/027—Nanofiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/26—Multiple-effect evaporating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/06—Flash distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B01D5/0036—Multiple-effect condensation; Fractional condensation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • 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
    • C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
    • 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
    • C02F1/048—Purification of waste water by evaporation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/06—Specific process operations in the permeate stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/08—Specific process operations in the concentrate stream
    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • 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
    • Y02A20/131—Reverse-osmosis

Abstract

A desalination apparatus is one equipped with multiple-effect evaporation unit; multiple heat-transfer pipes; a scale component removing means for removing at least portion of the scale component in raw water to thereby produce descaled water; mixed water feeding means for feeding a mixed water consisting of a mixture of raw water and descaled water as a water to be treated to the heat transfer tube of each of the evaporators of the first evaporator group disposed on the most anterior stage side among the multiple evaporator groups; and dilution water feeding means for feeding a dilution waterconsisting of a mixture of concentrated water and mixed water as a water to be treated to the heat transfer tube of each of the evaporators of the second evaporator group disposed on one low temperature side among the first evaporator group.

Description

The method of desalting plant and generation fresh water
Technical field
The present invention relates to be used to produce the structure of the desalting plant of fresh water.
Background technology
The currently known methods that is produced drinkable water by seawater comprises: for example in patent documentation 1 and 2 disclosed those.In these methods, produce drinkable water of condensation by following steps: utilize nanofiltration membrane that the fouling component is removed from former seawater, seawater and former sea water mixing with the gained fouling reduces supply to multiple-effect evaporator to distill described mixture with the gained mixture as raw water.
Patent documentation 1: Japanese uncensored patent disclosure No.2003-507183
Patent documentation 2:King Abdulaziz City for Science and Technology, Saudi Arabia, the patent No. 1000; 30/7/2006
Summary of the invention
The problem that the present invention is to be solved
Be contained in by supplying to fouling component such as the calcium sulfate in the water that multiple-effect evaporator handles, when its temperature raises and during the corresponding reduction of its solubleness, is deposited on easily on the surface of the heat-transfer pipe in the vaporizer.In order to prevent the deposition of calcium sulfate scaling, be necessary that the maximum operating temperature of vaporizer and the concentration rate value of untreated water are set to low as far as possible.This makes and to be difficult to produce effectively the pure water that is used to drink etc.
As described in patent documentation #1, in the method that produces fresh water, the scale deposition in the device that can not avoid evaporating fully.As a result, the thermo-efficiency of vaporizer reduces unfriendly, can not produce drinkable water of condensation effectively.Simultaneously, the claim of patent documentation #2 relates to utilizes the pretreated multi-effect distilling of nanofiltration (MED) or vapour compression distillation (VCD) type desalination system, and this desalination system is not specifically described.
Make the present invention so that the concrete structure based on the multiple-effect desalting plant that will protect system in the patent documentation 2 to be provided, make it possible to produce effectively water of condensation and prevent scale deposition simultaneously.
The method of dealing with problems
Above-mentioned purpose of the present invention can realize that described desalting plant comprises by desalting plant: the multiple-effect evaporator with a plurality of evaporating pots; With a plurality of heat-transfer pipes by its transmission steam; Wherein the outside surface by raw water being supplied to described a plurality of heat-transfer pipes is with by described raw material water generates steam and concentrated salt solution; Mode in the described heat-transfer pipe in the evaporating pot after being introduced in the steam that will produce in evaporating pot the preceding is connected to each other described a plurality of evaporating pots, thus make described steam can be used as described after the thermal source of evaporating pot; Be divided into a plurality of groups that are provided with respectively to the downstream from the upstream with described a plurality of evaporating pots.Described desalting plant also comprises: the fouling component-removal devices, and it removes at least a portion fouling component of being contained in the untreated former water to produce the water that the fouling component reduces; Mixing water supply arrangement, the mixture of the water that it reduces untreated former water and fouling component be as raw water, is supplied to the described heat-transfer pipe of each evaporating pot of the first evaporating pot group that is arranged in upstream in described a plurality of evaporating pot group; With the dilution water supply arrangement, it will be supplied to the position near the described heat-transfer pipe of temperature than each evaporating pot in the second evaporating pot group of the described first evaporating pot group of downside by the dilution water that mixes described concentrated salt solution and prepared by the prepared described mixture of described mixing water supply arrangement as raw water.
In this desalting plant, described dilution water supply arrangement preferably is configured to by being blended in the dilution water that the concentrated salt solution that produces in the described first evaporating pot group and described mixture prepare, and is supplied to the described heat-transfer pipe of each evaporating pot in the described second evaporating pot group.
Preferably each the described evaporating pot group except the described first and second evaporating pot groups includes and concentrates the salt solution supply arrangement, the concentrated salt solution that described concentrated salt solution supply arrangement will produce in any of the described a plurality of evaporating pot groups except the described first and second evaporating pot groups, as raw water, be supplied to the heat-transfer pipe of each evaporating pot.
Also preferred described dilution water supply arrangement is configured to by mixing by the concentrated salt solution that flash distillation produced, the concentrated salt solution that produces in the described second evaporating pot group and the dilution water that prepared by the prepared mixture of described mixing water supply arrangement, is supplied to the described heat-transfer pipe of each evaporating pot in the described second evaporating pot group.
Described fouling component-removal devices is nano-filtration membrane equipment preferably.
Above-mentioned purpose of the present invention can realize that described desalting plant comprises by a kind of method of utilizing desalting plant to produce fresh water: a plurality of evaporating pots and a plurality of heat-transfer pipes by its transmission steam; Wherein the outside surface by raw water being supplied to described a plurality of heat-transfer pipes is with by described raw material water generates steam and concentrated salt solution; Mode in the described heat-transfer pipe in the evaporating pot after being introduced in the steam that will produce in evaporating pot the preceding is connected to each other described a plurality of evaporating pots, thus make described steam can be used as described after the thermal source of evaporating pot; Be divided into a plurality of groups that are provided with respectively to the downstream from the upstream with described a plurality of evaporating pots.The method of described generation fresh water comprises that the fouling component removes step, and it removes at least a portion fouling component of being contained in the untreated former water to produce the water that the fouling component reduces; Mixing water supplying step, the mixture of the water that it reduces untreated former water and fouling component be as raw water, is supplied to the described heat-transfer pipe of each evaporating pot of the first evaporating pot group that is arranged in upstream in described a plurality of evaporating pot group; With the dilution water supplying step, its dilution water that will prepare by the described mixture that mixes described concentrated salt solution and prepare in described mixing water supplying step is supplied to the position near the described heat-transfer pipe of temperature than each evaporating pot in the second evaporating pot group of the described first evaporating pot group of downside as raw water.
The invention effect
The invention provides the method for desalting plant and generation fresh water, can produce water of condensation effectively and prevent scale deposition simultaneously by the untreated water of at high temperature operating desalting plant processing high concentration ratio value.
Description of drawings
Fig. 1 is the schematic block diagram that shows desalting plant according to an embodiment of the invention.
Fig. 2 is the schematic block diagram that shows the evaporating pot of the desalting plant shown in Fig. 1.
Fig. 3 is a schematic block diagram that changes scheme that shows the desalting plant shown in Fig. 1.
Fig. 4 is the schematic block diagram that shows another change scheme of the desalting plant shown in Fig. 1.
Fig. 5 is the schematic block diagram that shows another change scheme of the desalting plant shown in Fig. 1.
Fig. 6 is the schematic block diagram that shows another change scheme of the desalting plant shown in Fig. 6.
Fig. 7 is when by using the desalting plant shown in Fig. 1 that mixing water is carried out 2 times of schemas when concentrated.
Fig. 8 is when by using the desalting plant shown in Fig. 1 that mixing water is carried out 3 times of schemas when concentrated.
Fig. 9 is when by supplying with mixing water to the three evaporating pot groups mixing water being carried out 2 times of schemas when concentrated.
Figure 10 is when by supplying with mixing water to the three evaporating pot groups mixing water being carried out 3 times of schemas when concentrated.
Figure 11 is when by supplying with mixing water to the five evaporating pot groups mixing water being carried out 2 times of schemas when concentrated.
Figure 12 is when by supplying with mixing water to the five evaporating pot groups mixing water being carried out 3 times of schemas when concentrated.
Reference numeral is described
1 desalting plant
2 vaporizers
2a to 2t evaporating pot
The 3A first evaporating pot group
The 3B second evaporating pot group
3C the 3rd evaporating pot group
3D the 4th evaporating pot group
3E the 5th evaporating pot group
4 water tanks
5 fouling component-removal devices (nano-filtration membrane equipment)
6 mixing water supply arrangements
7 dilution water supply arrangements
8 condensers
9 concentrate the salt solution supply arrangement
The optimization model that carries out an invention
Hereinafter describe with reference to the accompanying drawings according to desalting plant of the present invention.Fig. 1 is the schematic block diagram of desalting plant according to an embodiment of the invention, and Fig. 2 is the schematic block diagram of the evaporating pot of desalting plant.Should illustrate that in order to promote to understand this device, each assembly in the accompanying drawing has all carried out partly zooming in or out, therefore not show its physical size.
As shown in Figure 1, desalting plant 1 comprises: hold untreated former water such as seawater water tank 4, remove the nano-filtration membrane equipment 5 that is included in the fouling component in the untreated former water, multiple-effect evaporator 2, will introduce driving vapour pipe 10, mixing water supply arrangement 6, dilution water supply arrangement 7 and condenser 8 in the vaporizer 2 by the high temperature driven steam that boiler (not shown) etc. produces.
Nano-filtration membrane equipment 5 is fouling component-removal devices, its remove be included in the water tank 4 in the former water that are untreated such as seawater that store to small part fouling component calcium sulfate (CaSO for example 4), with the water of generation fouling component minimizing, and be arranged between condenser 8 and the water tank 4.Nano-filtration membrane equipment 5 has mainly removes bivalent ions ability.Especially, preferably can remove the nano-filtration membrane equipment 5 of sulfate ion effectively.This equipment makes it possible to produce the water that the fouling component reduces, and wherein effectively removes the fouling component from supply to the former water of being untreated of nano-filtration membrane equipment (seawater).
Vaporizer 2 makes up by a plurality of evaporating pots that are connected in series (evaporating pot 2a to 2t), and as shown in Figure 2, each evaporating pot has: the evaporator room 21 of sealing, indirect heater 22 and be used to spray the nozzle 23 of raw water.The inside bottom of evaporator room 21 concentrates brinish as storage compartment and concentrates salt solution reservoir 24, and described concentrated salt solution is ejected into the raw water on the outside surface of the heat-transfer pipe 221 in the indirect heater 22 owing to produce with the evaporation that heat exchange caused of heat-transfer pipe 221 by making via nozzle 23.The inside bottom of evaporator room 21 also has: concentrate salt water inlet 26a, be used for being introduced in the concentrated salt solution that last evaporating pot produces; With concentrated brine outlet 26b, be used for will concentrate concentrated salt solution that salt solution reservoir 24 stores be expelled to after evaporating pot.The top of evaporator room 21 is provided with and is used for steam is discharged to outside vapour outlet 25a, and described steam is by carrying out heat exchange with heat-transfer pipe 221 and producing on heat-transfer pipe 221 outer surfaces.
Indirect heater 22 has: be arranged on arbitrary end that a plurality of heat-transfer pipes 221, first collector (header) 222 and second collector, 223, the first collectors 222 in the evaporator room 21 and second collector 223 are connected to described a plurality of heat-transfer pipe 221 separately.First collector 222 has: the 25b of steam-in portion is used for steam is introduced heat-transfer pipe 221; With condensing water inlet 27a, be used for guiding the water of condensation that in the heat-transfer pipe 221 of another evaporating pot, produces.Second collector 223 has condensation-water drain 27b, is used for discharging at heat-transfer pipe 221 by carrying out the water of condensation that heat exchange produces with heat-transfer pipe 221.When the amount of the water of condensation in being stored in first collector 222 surpassed predetermined amount, water of condensation was introduced second collector 223 by the inside of lowermost heat-transfer pipe 221.
The nozzle 23 that is arranged on indirect heater 22 tops is to be used for raw water is sprayed onto equipment on heat-transfer pipe 221 outside surfaces.
As shown in Figure 1, evaporating pot interconnects as follows: the vapour outlet 25a in the evaporating pot of upstream is connected to the steam-in 25b of next-door neighbour's evaporator downstream jar via vapour pipe 25, makes in the heat-transfer pipe 221 in the steam input next-door neighbour's that will produce in the evaporating pot of upstream the evaporator downstream jar as thermal source.Concentrated brine outlet 26b in the evaporating pot of upstream is via the concentrated salt water inlet 26a that concentrates in the evaporator downstream jar that brine tube 26 is connected to the next-door neighbour, makes to produce in the evaporating pot of upstream to be stored in the concentrated salt solution reservoir 24 that concentrates in the evaporator downstream jar that the concentrated salt solution input in the salt solution storage part 24 is close to then.Condensation-water drain 27b in the evaporating pot of upstream is connected to the condensing water inlet 27a in next-door neighbour's the evaporator downstream jar via condensate pipe 27, make will produce in the heat-transfer pipe in the evaporating pot of upstream 221 in first collector 222 of the indirect heater 22 in the evaporator downstream jar that the water of condensation input that is stored in then in second collector 223 is close to.
Be used for guiding driving vapour pipe 10 by the driving steam of generations such as boiler to be connected to the steam-in 25b of first collector 222 of the indirect heater 22 of upstream evaporating pot 2a.In the evaporating pot 2a of upstream, condensing water inlet 27a and concentrated salt water inlet 26a are not necessarily.
The vapour-discharge tube 51 that steam is guided to condenser 8 described below is connected to the vapour outlet 25a of second collector 223 of the indirect heater 22 among the evaporator downstream jar 2p, is used to discharge water of condensation to outside condensed water discharge pipe 53 and is connected to condensation-water drain 27b.In addition, the concentrated salt solution that is used for storing is expelled to outside concentrated salt water discharge pipe 54 and is connected to the concentrated brine outlet 26b that forms on the bottom of evaporator room 21.
A plurality of evaporating pots (evaporating pot 2a to 2t) in the vaporizer 2 of Gou Jianing are divided into from the upstream to a plurality of groups of arranged downstream thus.More specifically, described a plurality of evaporating pot is divided in the following order from the upstream to the first evaporating pot group 3A, the second evaporating pot group 3B, the 3rd evaporating pot group 3C, the 4th evaporating pot group 3D and the 5th evaporating pot group 3E of arranged downstream.Each evaporating pot group 3A to 3E all is configured to has 4 evaporating pots.Evaporating pot number among each evaporating pot group 3A to 3E can wait suitably according to design conditions to be selected.In this structure, be introduced among the first evaporating pot group 3A evaporating pot 2a that upstream end is provided with because will drive steam, so the service temperature among the first evaporating pot group 3A is the highest in five groups.Service temperature reduces to the 5th evaporating pot group 3E from the second evaporating pot group 3B.Service temperature in the evaporating pot of each evaporating pot group reduces downstream from the upstream.
Mixing water supply arrangement 6 will be by the fouling component water that reduces and the former water of supplying with from water tank 4 that is untreated that utilize nano-filtration membrane equipment 5 from the former water that is untreated, to remove to obtain to small part fouling component mixture as pending water, supply to the heat-transfer pipe in the evaporating pot of the first evaporating pot group 3A, the described first evaporating pot group 3A is arranged in the upstream of a plurality of evaporating pot group 3A to 3E.This mixing water supply arrangement 6 has supply pump (not shown) and mixing water supply-pipe 61, and described mixing water supply-pipe 61 is connected to the nozzle 23 of each evaporating pot 2a to 2d of the first evaporating pot group 3A.The part of the water supplying pipe 61 that the fouling component reduces is configured to passes the quencher moiety (not shown) that is arranged in the condenser 8, and the water that feasible fouling component of passing the water supplying pipe 61 of fouling component minimizing reduces is supplied to the refrigerant of the steam of condenser 8 as condensation.
Dilution water supply arrangement 7 will be by mixing the dilution water that the concentrated salt solution that produces among the second evaporating pot group 3B (being set to the first evaporating pot group 3A near low temperature side) and mixture by the preparation of mixing water supply arrangement prepare, as pending water, supply to the heat-transfer pipe among the evaporating pot 2e to 2h among the second evaporating pot group 3B.More specifically, dilution water supply arrangement 7 is provided with and concentrates brine tube 71, mixing water vent pipe 72 and supply pump (not shown), wherein concentrate the nozzle 23 that concentrated salt solution that brine tube 71 will be stored in the evaporating pot 2h that is arranged in the downstream part of the second evaporating pot group 3B causes each evaporating pot 2e to 2h of the second evaporating pot group 3B, mixing water vent pipe 72 will concentrate brine tube 71 and be connected to mixing water supply-pipe 61 and will cause via the partial confounding Heshui that mixing water supply arrangement 6 is supplied with and concentrate brine tube 71.This structure can reduce the concentration of the fouling component (for example calcium sulfate) in the pending water and be supplied to heat-transfer pipe 221 among the evaporating pot 2e to 2h among the second evaporating pot group 3B.
Each evaporating pot group 3C, 3D and 3E except the first evaporating pot group 3A and the second evaporating pot group 3B have concentrated salt solution supply arrangement, and its concentrated salt solution that will produce in any evaporating pot group except the first evaporating pot group 3A and the second evaporating pot group 3B is as pending water supply each evaporating pot to each evaporating pot group 3C, 3D, 3E.In the embodiment depicted in fig. 1, concentrated salt solution supply arrangement 9 among the 3rd evaporating pot group 3C is configured to: the concentrated salt solution that will be stored in the evaporating pot 2l that is arranged in the downstream side of the 3rd evaporating pot group 3C supplies to the evaporating pot 2i to 2l among the 3rd evaporating pot group 3C as pending water.Concentrated salt solution supply arrangement 9 among the 4th evaporating pot group 3D is configured to: the concentrated salt solution that will be stored in the evaporating pot 2p that is arranged in the downstream side of the 4th evaporating pot group 3D supplies to the evaporating pot 2m to 2p among the 4th evaporating pot group 3D as pending water.Concentrated salt solution supply arrangement 9 among the 5th evaporating pot group 3E is configured to: the concentrated salt solution that will be stored in the evaporating pot 2t that is arranged in the downstream side of the 5th evaporating pot group 3E supplies to the evaporating pot 2q to 2t among the 5th evaporating pot group 3E as pending water.Each concentrated salt solution supply arrangement 9 has supply pump (not shown) and concentrated salt water supplying pipe 91, concentrates salt water supplying pipe 91 and will concentrate the nozzle 23 that salt solution causes each evaporating pot of evaporating pot group 3C, 3D, 3E.
Condenser 8 is to utilize the mixing water pass mixing water supply-pipe 61 to cool off indirectly from the steam of the discharge section 25a discharge that is positioned at the downstream side evaporating pot 2t of multiple-effect evaporator 2 equipment with the generation water of condensation.The water of condensation that is produced is discharged to the outside via pipe 52.
Hereinafter describe to utilize desalting plant 1 to produce to be used for the method for the water of condensation of drinkable water etc. with said structure.At first will supply to vaporizer 2 via driving vapour pipe 10, will supply to vaporizer 2 by mixing fouling component water that reduces and the mixing water that the former water that is untreated obtains by mixing water supply arrangement 6 then by the driving steam of generations such as boiler.
The driving steam that supplies to vaporizer 2 is introduced the heat-transfer pipe 221 of the evaporating pot 2a be arranged in the upstream side of the first evaporating pot group 3A.To be fitted on the nozzle 23 among each evaporating pot 2a to 2d of the first evaporating pot group 3A by the mix moisture that mixing water supply arrangement 6 is supplied with, and be sprayed onto as pending water on the outside surface of heat-transfer pipe 221 of evaporating pot 2a to 2d.
The mixing water that is sprayed onto among the first evaporating pot group 3A on heat-transfer pipe 221 outside surfaces among the evaporating pot 2a of upstream carries out heat exchange with the driving steam that passes heat-transfer pipe 221 inside.Part mixing water evaporation, and gained steam caused heat-transfer pipe 221 among the evaporating pot 2b in the hithermost evaporator downstream jar as thermal source.And unevaporated mixing water becomes the concentrated salt solution of saltiness and the increase of fouling concentration of component on heat-transfer pipe 221 outside surfaces.Gained concentrates the flow downwards of salt solution along heat-transfer pipe 221, and is stored in the bottom of evaporator room 21 subsequently.Then, concentrate salt solution and be supplied to hithermost evaporator downstream jar 2b from concentrating brine outlet 26b via concentrated salt water supplying pipe 26.And, the driving steam that passes heat-transfer pipe 221 inside by be sprayed onto mixing water on heat-transfer pipe 221 outside surfaces and carry out heat exchange and be transformed into water of condensation.Water of condensation is stored in second collector 223 of indirect heater 22, causes first collector 222 of the indirect heater 22 among the hithermost evaporator downstream jar 2b then via condensate pipe 27.
In the evaporating pot 2b of the upstream evaporating pot 2a that is set to the contiguous first evaporating pot group 3A middle and lower reaches side, carry out heat exchange being sprayed onto the mixing water on heat-transfer pipe 221 outside surfaces from nozzle 23 and among hithermost upstream evaporating pot 2a, producing and pass between the steam of heat-transfer pipe 221 inside.This process produces steam and concentrated salt solution, and produces water of condensation in heat-transfer pipe 221.In 2c, the 2d of the first evaporating pot group 3A, carry out identical process successively.
The operation of the second evaporating pot group 3B is hereinafter described.To be sprayed onto on the outside surface of the heat-transfer pipe 221 among the evaporating pot 2e to 2h among the second evaporating pot group 3B by mixing is stored in the concentrated salt solution of the evaporating pot 2h that is arranged in the downstream part of the second evaporating pot group 3B and the mixing water introduced via mixing water mixing equipment 33 is prepared dilution water as pending water.At the evaporating pot 2e that is arranged in the upstream side of the second evaporating pot group 3B, the dilution water on being sprayed onto heat-transfer pipe 221 outside surfaces and in the first evaporating pot group 3A, produce and pass among the evaporating pot 2d of downstream part between the steam of heat-transfer pipe 221 inside and carry out heat exchange.This process produces the water of condensation in steam and concentrated salt solution and the heat-transfer pipe 221.Be arranged in the evaporating pot 2f of the second evaporating pot group 3B, carrying out heat exchange being sprayed onto the dilution water on heat-transfer pipe 221 outside surfaces from nozzle 23 and among hithermost upstream evaporating pot 2e, producing and pass between the steam of heat-transfer pipe 221 inside with the hithermost downstream part of upstream evaporating pot 2e.This produces the water of condensation in steam and concentrated salt solution and the heat-transfer pipe 221.In the subsequent evaporation jar 2g of the second evaporating pot group 3B and 2h, carry out identical process successively.
The concentrated salt solution that is stored in the evaporating pot 2l that is arranged in the downstream part of the 3rd evaporating pot group 3C is sprayed onto on the outside surface of heat-transfer pipe 221 of evaporating pot 2i to 2l of the 3rd evaporating pot group 3C.At the evaporating pot 2i that is arranged in the upstream side of the 3rd evaporating pot group 3C, carry out heat exchange being sprayed onto the concentrated salt solution on heat-transfer pipe 221 outside surfaces and in the evaporating pot 2h in the downstream side of the second evaporating pot group 3B, producing and pass between the steam of heat-transfer pipe 221 inside.This produces further concentrated salt solution that increases such as steam and saltiness and the water of condensation in the heat-transfer pipe 221.Be arranged in the evaporating pot 2j of the 3rd evaporating pot group 3C, carrying out heat exchange being sprayed onto the concentrated salt solution on heat-transfer pipe 221 outside surfaces from nozzle 23 and among hithermost upstream evaporating pot 2i, producing and pass between the steam of heat-transfer pipe 221 inside with the hithermost downstream side of evaporating pot 2i, upstream.This produces the water of condensation in steam and concentrated salt solution and the heat-transfer pipe 221.In other evaporating pot 2k of the 3rd evaporating pot group 3C and 2l, carry out identical process successively.
The 4th with the 5th evaporating pot group 3D and 3E in also repeat and identical process in the 3rd evaporating pot group 3C.
The water of condensation that produces in the heat-transfer pipe 221 in the evaporating pot 2a to 2t of vaporizer 2 is introduced in the evaporating pot in downstream successively via condensate pipe 27.At last, water of condensation is discharged via the condensation-water drain 27b of water shoot 53 from the evaporating pot 2t that is arranged in the downstream part of vaporizer 2 (the 5th evaporating pot group 3E evaporator downstream jar).And the steam that produces on heat-transfer pipe 221 surfaces among the evaporator downstream jar 2t in vaporizer 2 causes condenser 8 to change into water of condensation via vapour-discharge tube 51, discharges through pipe 52 then.The water of condensation of discharging from vaporizer 2 and can be used as drinkable water, process water and be used for the water of other application of various industries such as electron trade from the water of condensation that condenser 8 is discharged.
A concentrated brinish part that is stored among the evaporator downstream jar 2t in the vaporizer 2 is discharged to the outside via concentrated salt water discharge pipe 54 from concentrating brine outlet 26b.
The desalting plant 1 of this embodiment has following structure: the mixing water that wherein will have minimum fouling concentration of component is as pending water, be supplied to the evaporating pot 2a to 2d (wherein the fouling component such as calcium sulfate deposits easily) of the first evaporating pot group 3A that service temperature is the highest in all evaporating pot groups in evaporation-condensation process, to obtain water of condensation.This prevents on heat-transfer pipe 221 grades of scale deposition in evaporating pot 2a to 2d reliably.
In addition, because desalting plant 1 is configured to: the dilution water that will have low fouling concentration of component supplies to the evaporating pot 2e to 2h that has the second evaporating pot group 3B of second maximum operating temperature after the first evaporating pot group 3A, so can prevent reliably that also scale deposition is on the surface of heat-transfer pipe of the evaporating pot 2e to 2h of the second evaporating pot group 3B etc.
By preventing that reliably scale deposition from the surface of heat-transfer pipe 221 grades of evaporating pot, can prevent the reduction of heat transfer efficiency in the heat-transfer pipe 221.This has realized being used to drinking the effective generation with the water of condensation of other application.
Owing to can prevent the deposition of fouling, thus can further improve the temperature of the driving steam that supplies to vaporizer 2, with in addition higher operational temperature conditions and/or high concentration conditions under operation evaporating pot 2a to 2t.This allows effective real estate to give birth to a large amount of water of condensation.In addition, owing to the service temperature that can improve among the evaporating pot 2a to 2t, so can reduce the specific volume of the steam among the evaporating pot 2a to 2t.Therefore, can reduce the volume of evaporating pot 2a to 2t, therefore can reduce the size of desalting plant 1.
The part that to carry out the pending water of evaporation-condensation process in the evaporating pot 2e to 2h of the second evaporating pot group 3B is the mixture via the water of the be untreated former water and the minimizing of fouling component of mixing water vent pipe 72 supplies.Therefore, the flow of mixing water of waiting to supply to the evaporating pot 2a to 2d of the first evaporating pot group 3A can be remained on the level that the flow of the mixing water that will carry out the fresh water production process in whole desalting plant 1 can be carried out and increase simultaneously to the process that makes among the evaporating pot 2a to 2d with efficient manner.As a result, can produce the water of condensation that is used to drink with other application effectively by macro-mixing water.
Above described embodiment, but concrete structure of the present invention is not limited to these embodiments according to desalting plant 1 of the present invention.In this embodiment, dilution water supply arrangement 7 is configured to by mixing concentrated salt solution that produces among the second evaporating pot group 3B and the dilution water that the mixing water of introducing via mixing water vent pipe 72 prepares, and supplies to the heat-transfer pipe of the evaporating pot in the second evaporating pot group.Yet, for example as shown in Figure 3, can be constructed as and to supply to the heat-transfer pipe among the evaporating pot 2e to 2h among the second evaporating pot group 3B by mixing concentrated salt solution that produces in the first evaporating pot group and the dilution water that the mixing water of supplying with via mixing water vent pipe 72 prepares.
As shown in Figure 1, this embodiment is configured to and will be provided with the concentrated brinish part that produces and store among the evaporating pot group 3C, the 3D that concentrate salt solution supply arrangement 9 and the 3E as pending water, via concentrating the evaporating pot that salt solution supply arrangement 9 supplies to evaporating pot group 3C, 3D and 3E.Yet, the invention is not restricted to this structure.For example, as shown in Figure 3, concentrating salt solution supply arrangement 9 can be constructed as: the concentrated brinish part that will produce and store in the evaporator downstream jar 2h of evaporating pot group 3B, 3C that being provided with of the next-door neighbour upstream of evaporating pot group 3C, 3D and 3E concentrates salt solution supply arrangement 9 and 3D, 2l, 2p supplies to each evaporating pot.
This embodiment is configured to and will only supplies to the evaporating pot 2e to 2h of the second evaporating pot group 3B by the dilution water that mixes concentrated salt solution and mixing water preparation; Yet structure of the present invention is not limited thereto.For example, when in the evaporating pot 2i to 2l of the 3rd evaporating pot group 3C, also exist forming fouling for example during the risk of calcium sulfate, can adopt wherein and will also supply to the structure of the evaporating pot 2i to 2l of the 3rd evaporating pot group 3C by mixing the dilution water that concentrates salt solution and mixing water preparation.
In this embodiment, can also adopt following structure, wherein for example as shown in Figure 4, preliminary heating device 100 is set as the equipment that is used to heat the mixing water that passes mixing water supply-pipe 61.Fig. 4 has shown that the steam that produces among the evaporating pot 2e to 2t that wherein utilizes in the second evaporating pot group 3B to the, five evaporating pot group 3E heats the structure of mixing water as thermal source.This structure makes to raise effectively and is sprayed onto the temperature of the heat-transfer pipe 221 lip-deep mixing waters among the evaporating pot 2a to 2d among the first evaporating pot group 3A, and reduces mixing water and pass the temperature difference between the driving steam of heat-transfer pipe 221 of evaporating pot 2a to 2d.This has increased the quantity of steam that produces among the evaporating pot 2a to 2d, thereby can produce water of condensation effectively by mixing water.
Perhaps, this embodiment can have following structure: wherein be provided with reverse osmosis membrane equipment (RO equipment), the water that the feasible fouling that will pass nano-filtration membrane equipment 5 reduces is as raw water, be supplied to reverse osmosis membrane equipment (RO equipment) and produce pure water, the RO salt solution and the former water that is untreated that utilizes reverse osmosis membrane equipment (RO equipment) to produce by mixing produces mixing water simultaneously, then with this mixing water as the evaporating pot 2a to 2d of pending water supply to the first evaporating pot group 3A.This makes and also can produce the water that is used to drink by reverse osmosis membrane equipment, thereby realizes effective generation of fresh water.If necessary, seawater and the extra mixing solutions of having crossed by nanofiltration membrane treatment of RO brinish can also be supplied to the evaporating pot 2a to 2d of the first evaporating pot group 3A.
In the embodiment depicted in fig. 1, when the pressure height that passes the driving steam that drives vapour pipe 10 when being enough to be compressed in the steam that produces in any evaporating pot in the vaporizer 2, can adopt the structure that shows among Fig. 5, vapor recompression injector 101 wherein can be set in driving the stream of vapour pipe 10 and the part of the steam that produces can be supplied to vapor recompression injector 101 in evaporating pot.In Fig. 5, the part of the steam that produces in will the evaporator downstream jar 2d in the first evaporating pot group 3A is supplied to vapor recompression injector 101 via vapour-discharge tube 102.In this structure, the steam that produces in evaporating pot 2d can be used as the thermal source of other evaporating pot 2a to 2c that is used to be positioned at evaporating pot 2d upstream.Therefore, the water of condensation (product water) that utilizes less evaporating pot to obtain to expect.By basic identical divided by the value and the service temperature difference between the adjacent evaporating pot of the number gained of evaporating pot with the operating temperature range of vaporizer 2 (it is poor corresponding to the service temperature between upstream evaporating pot 2a and the evaporator downstream jar 2t).Therefore, necessary evaporating pot is few more, and the service temperature difference between the then adjacent evaporating pot is big more.This structure allows to produce the water of condensation that is used to drink etc. effectively by mixing water.The evaporating pot that links to each other with vapour-discharge tube 102 can wait suitably according to design conditions and select.
Can also adopt the structure that shows among Fig. 6 for example, wherein be provided with a plurality of vapor recompression injectors 101, and the steam that will produce is supplied to one in a plurality of vapor recompression injectors 101 in different evaporating pot 2d, 2h.The driving steam that passes a vapor recompression injector 101 is introduced in the heat-transfer pipe 211 among the upstream evaporating pot 2a among the first evaporating pot group 3A, and the driving steam that will pass another vapor recompression injector 101 is introduced among the first evaporating pot group 3A in those except the heat-transfer pipe 211 of upstream evaporating pot 2a.
In this embodiment, for prevent soft junction dirt as tosca in evaporating pot, can after acid being added untreated former water such as seawater, carry out the decarbonate process.
In this embodiment, can also adopt following structure: wherein have the pressure regulating equipment of inner pressure relief that the concentrated salt solution that will produce imports the flash pipe among the evaporating pot 2e to 2h of the second evaporating pot group 3B and is used to make the evaporating pot 2e to 2h of the second evaporating pot group 3B in the first evaporating pot group 3A, and the concentrated salt solution that will produce supplies to the evaporating pot 2e to 2h of the second evaporating pot group 3B to carry out flash distillation in the first evaporating pot group 3A.This structure can more effectively produce the water of condensation that is used to drink with other application.When adopting this structure, the concentrated salt solution that dilution water supply arrangement 7 will produce by flash distillation, by carrying out the concentrated salt solution that heat exchange produces with heat-transfer pipe 211 and comprising the heat-transfer pipe that supplies to the evaporating pot 2e to 2h among the second evaporating pot group 3B via the dilution water of the mixing water of mixing water vent pipe 72 introducings.
The inventor is by having confirmed above-mentioned effect as hereinafter calculating solubility product.The water that has a same nature when use is when waiting to be supplied to the raw water of desalting plant, and the liquid supply method that can produce water of condensation as much as possible (product water) in not causing the sedimentary scope of structure is adopted in expectation.In other words, if the concentration rate value of the pending water of the multiple-effect evaporator 2 of can increasing supply then can more effectively obtain product water.Effective generation of the water of condensation of realizing by desalting plant 2 according to the present invention and the method that produces fresh water (product water) is hereinafter described.Water (NF product water) that the fouling component that the common former water that is untreated (seawater is untreated), its fouling component have been removed by nano-filtration membrane equipment 5 parts of showing table 1 reduces and the fouling component concentrations in the RO salt solution.For the water quality of NF product water in the table 1, shown and utilized the NF film of making by Dow ChemicalCompany (XUS-229323), the fouling component concentrations in the NF water of generation as nano-filtration membrane equipment 5.For RO brinish water quality, shown that utilization is by the fouling component concentrations in the RO salt solution of reverse osmosis membrane equipment (RO equipment) generation of the RO film (SW30HRLE-400) of DowChemical Company manufacturing.
Table 1
The fouling component Untreated water The NF product water RO salt solution
??Ca(ppm) ??480 ??180 ??1025
??SO 4(ppm) ??3200 ??100 ??255
??Cl(ppm) ??23000 ??21000 ??46740
??TDS(ppm) ??102000 ??33000 ??77545
Utilize by with the prepared mixing water of the untreated seawater shown in the certain proportion mixture table 1 (untreated water), NF product water and RO salt solution as the mixing water that supplies to the evaporating pot 2a to 2d among the first evaporating pot group 3A via mixing water supply arrangement 6.Especially, this mixing water comprises the untreated seawater (untreated water) of 55wt%, the NF product water of 18wt% and the RO salt solution of 27wt%.Fouling component concentrations in the consequent mixing water is shown in Table 2.
Table 2
The fouling component Mixing water
??Ca(ppm) ??411
??SO 4(ppm) ??1849
??Cl(ppm) ??29050
??TDS(ppm) ??49977
Table 3 illustrates when utilizing desalting plant 1 with structure shown in Figure 1 to produce water of condensation (product water) by the mixing water with the concentration of component of fouling shown in the table 2 with 24000 tons/day speed, evaporation in the evaporating pot and service temperature (vaporization temperature).Table 3 shows evaporation and the service temperature (vaporization temperature) of upstream evaporating pot 2a, 2e, 2i, 2m and 2q among as an example the evaporating pot group 3A to 3E.As shown in fig. 1, heating steam is supplied to upstream evaporating pot 2a among the first evaporating pot group 3A, and the evaporator downstream jar 2t of the upstream evaporating pot 2a of the temperature and pressure in the evaporating pot from the first evaporating pot group 3A in the 5th evaporating pot group 3E reduces gradually.In evaporating pot group 3A to 3E, supply in each evaporating pot with parallel mode pending water and make the steam output in the evaporating pot identical, so the concentrated brinish concentration on the tube surface is also identical in the evaporating pot.Evaporating pot 2a, the 2e, 2i, 2m and the 2q that show in the table 3 are the easiest evaporating pots that scale deposition occurs in all evapn jar group.
Table 3
The evaporating pot group The 1st of the 1st evaporating pot group is steamed The 5th of the 2nd evaporating pot group is steamed The 9th of the 3rd evaporating pot group is steamed The 13rd of the 4th evaporating pot group is steamed The 17th of the 5th evaporating pot group is steamed
Send out jar (2a) Send out jar (2e) Send out jar (2i) Send out jar (2m) Send out jar (2q)
Steam output (kg/h) ??50000 ??50000 ??50000 ??50000 ??50000
Vaporization temperature (℃) ??125 ??109 ??93.5 ??77.5 ??61.5
Table 4 shows that working as the mixing water with the concentration of component of fouling shown in the table 2 evaporates-concentration process in desalting plant 1, under evaporation conditions as shown in table 3 (being vaporization temperature and steam output), become 2 or at 3 o'clock until its concentration rate value, the calculation result of solubility product.Fig. 7 is the schema when the concentration rate value in the desalting plant 1 is 2.Fig. 8 is the schema when the concentration rate value in the desalting plant 1 is 3.Herein in the calculating of solubility product, suppose that the flow that causes the mixing water of dilution water supply arrangement 7 from mixing water supply arrangement 6 is 0.
Table 4 show the concentrated solution on the tube surface in the evaporating pot maximum concentration (total dissolved solids, TDS), the solubility product and the highest tolerable solubility product of calcium ion and sulfate ion.When device run duration solubility product surpassed the highest tolerable solubility product, scale deposition appearred.Herein, based on (the United State Department ofInterior of salt solution office of the U.S. Ministry of Internal Affairs, Office of Saline Water) technical data handbook (14.16 pages of 1A of OSW, 14.16 value ([Ca] * [SO of the highest tolerable solubility product that shows among the figure of scaling system 4 page or leaf 1B), 4]).Yet, these data are to measure by (anhydrous) calcium sulfate being dissolved in be untreated former water and the concentrated salt solution with the limit of determining solubility product, therefore are difficult to be applied directly to the situation that the mixture of water that the fouling component is reduced and untreated former water (untreated former seawater) is handled as raw water.When utilizing the muriate component concentrations to compare as a reference, the data of salt solution office of the U.S. Ministry of Internal Affairs have more been obtained under the exacting terms at the water that reduces than fouling.Therefore, in judging solubility limit, there is not the problem of makeshift, so can be safer.In order to estimate solubility product more accurately, the ionic strength that can use raw water as a reference.
The calculating of the solubility product in the table 4 is described below.The method that with concentration rate value in the desalting plant is the solubility product among the evaporating pot 2a that determined among the first evaporating pot group 3A at 2 o'clock is set forth as an example.According to Fig. 7, can obtain to supply to the flow of the mixing water of the evaporating pot 2a among the first evaporating pot group 3A by following formula: (2000 tons/hour)/4 evaporating pots=500 ton/hour can obtain the steam flow that produces among the evaporating pot 2a by following formula: (200 tons/hour)/4 evaporating pots=50 ton/hour.Therefore, can obtain concentration rate value (500 tons/hour)/(500 tons/hour-50 tons/hour)=1.1111 among the evaporating pot 2a by following formula.Therefore, the concentrated brinish calcium concentration of component among the evaporating pot 2a is 411 * 1.1111=457ppm, and the sulfate ion component concentrations is 1849 * 1.1111=2054ppm.Therefore, can obtain the calcium component concentration by following formula: 457/40/1000=0.011425 mol (wherein 40 is nucleidic mass of calcium), and can obtain the sulfate ion component by following formula: 2054/96/1000=0.021396 mol (wherein 96 is molecular weight of sulfate ion).Therefore, the solubility product of calcium sulfate is (calcium component) * (sulfate ion component)=0.011425 * 0.021396=0.000244.
Table 4
Figure G2007800530792D00161
Clearly visible as result displayed from table 4, the calcium ion in all evapn jar 2a, 2e, 2i, 2m and the 2q of the upstream side of the evaporating pot group 3A to 3E that lays respectively at easy deposition fouling component and the solubility product of sulfate ion all are lower than the highest tolerable solubility product.This shows, even desalting plant does not exist the tube surface of scale deposition in evaporating pot and the risk at other parts place in for example 125 ℃ of operations down of high temperature condition yet.Therefore, the desalting plant of this embodiment has realized being used to drinking the effective generation with the water of condensation (product water) of other application.
For relatively, calculate and supply to mixing water under the situation of the evaporating pot among the 3rd evaporating pot group 3C and mixing water is supplied to solubility product under the situation of the evaporating pot among the 5th evaporating pot group 3E.Table 5 and 6 illustrates the result.Concentration rate value in the desalting plant 1 is 2 or 3.Fig. 9 is to be schema when just mixing water supplies to evaporating pot among the 3rd evaporating pot group 3C under 2 the situation in the concentration rate value of supposition in the desalting plant 1, and Figure 10 is that the concentration rate value is 3 o'clock a schema.Figure 11 is the schema when the concentration rate value of supposition in the desalting plant 1 is the evaporating pot that under 2 the situation mixing water is supplied among the 5th evaporating pot group 3E, and Figure 12 is that the concentration rate value is 3 o'clock a schema.
Table 5
Figure G2007800530792D00172
Figure G2007800530792D00181
Table 6
Figure G2007800530792D00182
Figure G2007800530792D00191
Clearly visible as result displayed from table 5 and 6, when mixing water being supplied to the 3rd and the 5th evaporating pot group 3C and 3E, be all to have observed the deposition of fouling on tube surface under two kinds of situations of 2 and 3 in the concentration rate value.This shows, is used to drink or the water of condensation (product water) of other purposes in order to produce effectively, and it is necessary that control concentration rate value is not more than 2.

Claims (6)

1. desalting plant comprises:
Multiple-effect evaporator with a plurality of evaporating pots; With
A plurality of heat-transfer pipes by its transmission steam;
Wherein the outside surface by raw water being supplied to described a plurality of heat-transfer pipes is with by described raw material water generates steam and concentrated salt solution;
Mode in the described heat-transfer pipe in the evaporating pot after being introduced in the steam that will produce in evaporating pot the preceding is connected to each other described a plurality of evaporating pots, thus make described steam can be used as described after the thermal source of evaporating pot; With
Described a plurality of evaporating pot is divided into a plurality of groups that are provided with respectively to the downstream from the upstream;
Described desalting plant also comprises:
The fouling component-removal devices, it removes at least a portion fouling component of being contained in the untreated former water to produce the water that the fouling component reduces;
Mixing water supply arrangement, the mixture of the water that it reduces untreated former water and fouling component be as raw water, is supplied to the described heat-transfer pipe of each evaporating pot of the first evaporating pot group that is arranged in upstream in described a plurality of evaporating pot group; With
The dilution water supply arrangement, it will be supplied to the position near the described heat-transfer pipe of temperature than each evaporating pot in the second evaporating pot group of the described first evaporating pot group of downside by the dilution water that mixes described concentrated salt solution and prepared by the prepared described mixture of described mixing water supply arrangement as raw water.
2. desalting plant according to claim 1, wherein said dilution water supply arrangement is designed to be supplied to the described heat-transfer pipe of each evaporating pot in the described second evaporating pot group with by being blended in concentrated salt solution that produces in the described first evaporating pot group and the dilution water that is prepared by the prepared described mixture of described mixing water supply arrangement.
3. desalting plant according to claim 2, wherein each the described evaporating pot group except the described first and second evaporating pot groups includes and concentrates the salt solution supply arrangement, the concentrated salt solution that described concentrated salt solution supply arrangement will produce in any of the described a plurality of evaporating pot groups except the described first and second evaporating pot groups, as raw water, be supplied to the described heat-transfer pipe of each evaporating pot of same evaporating pot group.
4. desalting plant according to claim 1 also comprises flashing apparatus, and its concentrated salt solution that will produce in the described first evaporating pot group is supplied to each evaporating pot in the described second evaporating pot group to carry out flash distillation; With
Described dilution water supply arrangement is configured to by mixing by the concentrated salt solution that flash distillation produced, the concentrated salt solution that produces in the described second evaporating pot group and the dilution water that prepared by the prepared mixture of described mixing water supply arrangement, is supplied to the described heat-transfer pipe of each evaporating pot in the described second evaporating pot group.
5. according to each described desalting plant in the claim 1～4, wherein said fouling component-removal devices is a nano-filtration membrane equipment.
6. one kind by utilizing desalting plant to produce the method for fresh water, and described desalting plant comprises: a plurality of evaporating pots and a plurality of heat-transfer pipes by its transmission steam;
Wherein the outside surface by raw water being supplied to described a plurality of heat-transfer pipes is with by described raw material water generates steam and concentrated salt solution;
Mode in the described heat-transfer pipe in the evaporating pot after being introduced in the steam that will produce in evaporating pot the preceding is connected to each other described a plurality of evaporating pots, thus make described steam can be used as described after the thermal source of evaporating pot; With
Described a plurality of evaporating pot is divided into a plurality of groups that are provided with respectively to the downstream from the upstream;
The method of described generation fresh water comprises:
The fouling component is removed step, and it removes at least a portion fouling component of being contained in the untreated former water to produce the water that the fouling component reduces;
Mixing water supplying step, the mixture of the water that it reduces untreated former water and fouling component be as raw water, is supplied to the described heat-transfer pipe of each evaporating pot of the first evaporating pot group that is arranged in upstream in described a plurality of evaporating pot group; With
The dilution water supplying step, its dilution water that will prepare by the described mixture that mixes described concentrated salt solution and prepare in described mixing water supplying step is supplied to the position near the described heat-transfer pipe of temperature than each evaporating pot in the second evaporating pot group of the described first evaporating pot group of downside as raw water.
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CN102329037A (en) * 2011-10-24 2012-01-25 哈尔滨锅炉厂有限责任公司 Low-temperature multi-effect evaporation sea water desalting device and sea water desalting method
CN102329037B (en) * 2011-10-24 2015-07-29 哈尔滨锅炉厂有限责任公司 Low-temperature multi-effect evaporation seawater desalinization device and method for desalting seawater
CN103170149A (en) * 2011-12-22 2013-06-26 日立造船株式会社 Multi-effect type evaporation method and multi-effect type evaporation device
CN103170149B (en) * 2011-12-22 2015-12-09 日立造船株式会社 Multiple effectiveness formula method of evaporating and multiple effectiveness formula vaporising device
CN103641192A (en) * 2013-12-24 2014-03-19 上海电气电站设备有限公司 Multi-tube-bundle arrangement structure of low-temperature multi-effect sea water desalination evaporator
CN103641192B (en) * 2013-12-24 2015-12-30 上海电站辅机厂有限公司 Low-temperature multiple-effect seawater desalination evaporator multitubular bundles arrangement

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