CN102976504A - Sea water desalination system - Google Patents

Sea water desalination system Download PDF

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Publication number
CN102976504A
CN102976504A CN2012102659601A CN201210265960A CN102976504A CN 102976504 A CN102976504 A CN 102976504A CN 2012102659601 A CN2012102659601 A CN 2012102659601A CN 201210265960 A CN201210265960 A CN 201210265960A CN 102976504 A CN102976504 A CN 102976504A
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polyose
mentioned
water
cleaning
treatment device
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CN102976504B (en
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荒户利昭
隅仓岬
阴山晃治
馆隆广
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Hitachi Ltd
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Hitachi Ltd
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    • 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

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  • Water Treatment By Sorption (AREA)

Abstract

In a sea water desalination system using reverse osmosis membrane, polysaccharose compositions in the sea water is steadily removed, and performance of the reverse osmosis membrane is kept. The sea water desalination system (100A) employs the reverse osmosis membrane in a reverse osmosis membrane sea water desalination device (18) to carry out sea water desalination. Sea water supplied to the reverse osmosis membrane sea water desalination device (18) is processed by a polyose adsorption processing device (16 (16A and 16B)), and polyose including TEP is adsorbed and removed. The polyose adsorbed on the polyose adsorption processing device (16 ) is washed by cleaning water supplied by a clean water supply device (19). And the cleaning condition is determined by polyose density of the sea water before and after being processed by the polyose adsorption processing device (16).

Description

The seawater desalination system
Technical field
The present invention relates to use reverse osmosis membrane to obtain the seawater desalination system of fresh water from seawater.
Background technology
In recent years, the tendency that exists seawater desalination treatment system to increase, this seawater desalination treatment system constitute and comprise the reverse osmosis membrane processing device that has utilized the filtration treatment that dependence reverse osmosis (RO:Reverse Osmosis) film carries out.Reverse osmosis membrane is made by the starting material of Mierocrystalline cellulose or polymeric amide etc.The reverse osmosis membrane processing device makes it pass through reverse osmosis membrane by the pressure more than 2 times that seawater is applied its seepage water pressure, thereby suppresses seeing through of salinity, can obtain fresh water.Cause one of phenomenon that the through performance of reverse osmosis membrane processing device reduces that the aquatic organism dirt is arranged.
Said aquatic organism dirt (Fouling) refers to the aquatic organism dirt (tamper) by the extracellular metabolic product generation of microorganism generation contained in the seawater.For the generation of aquatic organism dirt, be known that among the biomacromolecule material, for example organism of plant plankton origin particularly have adhesive TEP (Transparent Exopolymer Particles; Transparent extracellular polymer body particle) proportion large (for example with reference to aftermentioned non-patent literature 1).TEP is a kind of of polyose.
In addition, in patent documentation 1, put down in writing that the contrary Cleaning Line at pretreating device possesses the opacity meter, adjusts the desalination device (corresponding with the application " seawater desalination system ") of rinse water feed rate and the purging method of pretreating device according to opacity in the seawater desalination system.In patent documentation 2, put down in writing in the pretreating device that the dirty matter of desalination device is partly removed and disposed the heating part so that the technology that the cleaning efficiency of pretreating device improves at back washing line (cleaning water system).In patent documentation 3, put down in writing in relying on the water treatment method of reverse osmosis membrane and to have come technology that organism is adsorbed for replacing life-span of prolonging reverse osmosis membrane, with gac.
The look-ahead technique document
Patent documentation
Patent documentation 1: TOHKEMY 2007-014902 communique
Patent documentation 2: TOHKEMY 2011-031121 communique
Patent documentation 3: TOHKEMY 2010-234353 communique
Non-patent literature
Non-patent literature 1: in the bamboo, " pre-treatment of RO seawater desalination and aquatic organism dirt ", Sea of Japan hydrotechnics can will,, the 63rd volume, pp.367-371 in 2009
Summary of the invention
Invent problem to be solved
In order to obtain the high-efficient operation of seawater desalination system, aquatic organism dirt countermeasure is necessary.As the aquatic organism dirt countermeasure of the reverse osmosis membrane processing device of seawater desalination system, for example known have a following methods, that is: by having utilized ultra-filtration membrane { UF (Ultrafiltration; Ultrafiltration) film } pretreatment procedure in the leading portion side of reverse osmosis membrane TEP is reduced, thereby the performance that prevents reverse osmosis membrane reduces.Yet, even by the pretreatment procedure that utilizes the UF film, also polyose, particularly TEP can't be removed fully, therefore exist the performance that can't prevent reverse osmosis membrane to reduce such problem.
The object of the invention is to solve the problem of above-mentioned conventional art, following seawater desalination system is provided, that is: by the leading portion side at the reverse osmosis membrane processing device polyose is stably removed, the performance that can prevent the reverse osmosis membrane that causes because of the aquatic organism dirt reduces, prolong the replacing life-span of reverse osmosis membrane, so that reduce as the operating cost of entire system.
Be used for solving the means of problem
In order to solve above-mentioned problem, seawater desalination system involved in the present invention is a kind of seawater desalination system that uses reverse osmosis membrane, it is characterized in that possessing: pretreating device, and this pretreating device carries out pre-treatment to the seawater that water intaking obtains; The polyose absorbing treatment device, this polyose absorbing treatment device uses the polyose sorbing material, and contained polyose composition in the first processing water that was undertaken by above-mentioned pretreating device processing is carried out Adsorption; With the reverse osmosis membrane processing device, this reverse osmosis membrane processing device uses above-mentioned reverse osmosis membrane, and the second processing water of having been removed above-mentioned polyose composition by above-mentioned polyose absorbing treatment device is carried out desalination; Described seawater desalination system also possesses: polyose concentration measuring mechanism, this polyose concentration measuring mechanism are measured the second polyose concentration of processing the first polyose concentration in the water and removed polyose composition the second processing water afterwards by the polyose absorbing treatment device from first of pretreating device; Cleaning condition determination means, this cleaning condition determination means determine the cleaning condition of polyose sorbing material based on the first polyose concentration and the second polyose concentration measured by the polyose concentration measuring mechanism; And wiper mechanism, this wiper mechanism cleans the polyose sorbing material based on the cleaning condition that is determined by the cleaning condition determination means.
According to the present invention, decide cleaning condition for the polyose sorbing material owing to process the first polyose concentration of water and second the second polyose concentration of processing water based on first before and after the polyose Transformatin that relies on the polyose absorbing treatment device, so, can according to the variation that lasts of the polyose absorption property of polyose absorbing treatment device, clean with suitable cleaning condition.In addition, by with suitable cleaning condition the polyose absorbing treatment device being cleaned, can keep the polyose absorption property of polyose absorbing treatment device, thereby can prevent the diactinic reduction of reverse osmosis membrane.
In addition, preferably, set a plurality of polyose absorbing treatment devices with respect to a reverse osmosis membrane processing device, constitute, during by a polyose absorbing treatment device of wiper mechanism cleaning, carry out the Adsorption of polyose composition by another one polyose absorbing treatment device at least, can continue to carry out the second supply of processing water with respect to the reverse osmosis membrane processing device.
And then the cleaning condition determination means determines that in the temperature of flow velocity, rinse water of rinse water that the polyose sorbing material is cleaned and the scavenging period at least one is as cleaning condition.
The effect of invention
According to the present invention, following seawater desalination system can be provided, that is: by the leading portion side at the reverse osmosis membrane processing device polyose is stably removed, the performance that can prevent the reverse osmosis membrane that causes because of the aquatic organism dirt reduces, prolong the replacing life-span of reverse osmosis membrane, reduce the operating cost as entire system.
Description of drawings
Fig. 1 is the summary pie graph of the related seawater desalination system 100A of the first embodiment.
Fig. 2 be the processing water yield of expression in the absorbing treatment device 16 with process after the second graphic representation of processing the relation of the TEP concentration in the water.
Fig. 3 is the cleaning model of expression experimental result and the TEP concentration ratio C/C at circulation end 0The graphic representation of variation.
Fig. 4 is the graphic representation that represents respectively to rely on the organic change in concentration before and after the adsorption treatment that polyose absorbing treatment device 16 carries out by material.
Fig. 5 is the summary pie graph of the related seawater desalination system 100B of the modified example of the first embodiment.
Fig. 6 is the summary pie graph of the related seawater desalination system 600 of the second embodiment.
Embodiment
Be elaborated referring to the embodiment of accompanying drawing to seawater desalination system involved in the present invention.
" the first embodiment "
(the whole summary of seawater desalination system 100A)
Fig. 1 is the summary pie graph of the related seawater desalination system 100A of the first embodiment.
Seawater desalination system 100A constitutes and comprises water pump P1, water intaking groove 12, filtration pump P2, pretreating device 14, polyose absorbing treatment device 16 is (among Fig. 1 with 16A, 16B represents), husky filtration unit 30 is (among Fig. 1 with 30A, 30B represents), process tank 15, supply pump P3, high-pressure pump P4, reverse osmosis membrane type seawater desalination device 18, water analysis outfit (polyose concentration measuring mechanism) 17, cleaning condition calculation apparatus (cleaning condition determination means) 171A, rinse water supply device 19, rinse water heating unit 190A, switching control 31, switching valve VA 1～VA 5, VB 1～VB 5, also have rinse water supplying tubing 191A, 191B, 192A, 192B, sampling pipe arrangement 122,160A, 160B, 162A, 162B etc. in addition.
Between water analysis outfit 17 and the switching control 31, between switching control 31 and the cleaning condition calculation apparatus 171A, between water analysis outfit 17 and the cleaning condition calculation apparatus 171A, between cleaning condition calculation apparatus 171A and the rinse water supply device 19, between cleaning condition calculation apparatus 171A and the rinse water heating unit 190A, between switching control 31 and the rinse water heating unit 190A, utilize respectively communication circuit to connect.
Water intaking groove 12 is used for the seawater SW that is fetched from the sea by water pump P1 is carried out temporary transient water storage.Pretreating device 14 is filtration units suitable with husky filtration treatment, for example is to divide the filtration unit of removing from seawater with inclusion and the dirty matter of 1 μ m～100 μ m sizes.In pretreating device 14, for example use MF (Microfiltration) film.From water intaking groove 12 to pretreating device 14, carry out sea water supply by filtration pump P2, filtered by the MF film forcibly by the outlet pressure of filtration pump P2.The MF film of pretreating device 14 is for example suitably by back washing, but is not characteristic of the present invention at this, omits at Fig. 1 so be used for the pipe arrangement etc. of back washing, and also the description thereof will be omitted.
At this, seawater desalination system 100A is before will be in pretreating device 14 processed seawater (first processes water) is supplied with to reverse osmosis membrane type seawater desalination device (reverse osmosis membrane processing device) 18, processed by polyose absorbing treatment device 16, for this processed seawater (second processes water) is supplied with to reverse osmosis membrane type seawater desalination device 18, possess a plurality of polyose absorbing treatment devices 16 and the group (being 2 groups in present embodiment shown in Figure 1) that is disposed at the husky filtration unit 30 of its back segment.
Polyose absorbing treatment device 16 for example is made of the airtight container of the top tegmentum of stainless steel, and its inside comprises: lower cavity 16a, as processing the space that water flows into for first; For example the granular layer of natural zeolite by not shown sorbing material supporting grid spare supporting, is used as the polyose sorbing material 16b of lamination mineral thereon; Upper cavity 16c is the space of the processing water on it being received water.
Sorbing material supporting grid by eyelet than polyose absorbing treatment device 16 do not fall the particle of such polyose absorbing treatment device 16 little, such as the net of stainless steel or the porous plate of pottery system etc. consist of.
Husky filtration unit 30 is used for and will removes from the polyose sorbing material 16b that polyose absorbing treatment device 16 flows out, for example consisted of by the airtight container of the top tegmentum of stainless steel, its inside comprises: upper cavity 30a, as the space that flows into for the second processing water of processing and discharge by polyose absorbing treatment device 16; Husky filtering material 30b, by not shown filter material supporting grid spare supporting and by lamination thereon; Lower cavity 30c is the space of the processing water under it being received water.
In the pipe arrangement of the outlet that connects pretreating device 14 and the lower cavity 16a of polyose absorbing treatment device 16A, more leaning on the position in downstream side (polyose absorbing treatment device 16A side) that switching valve VA is being set than branching portion 1, the branching portion branch of above-mentioned pipe arrangement and with pipe arrangement that the lower cavity 16a of polyose absorbing treatment device 16B is connected in switching valve VB is set 1
In addition, in the upper cavity 16c that connects polyose absorbing treatment device 16A and pipe arrangement that the upper cavity 30a of husky filtration unit 30A is connected, switching valve VA is set 2, in the pipe arrangement of the upper cavity 30a of the upper cavity 16c that connects polyose absorbing treatment device 16B and husky filtration unit 30B, switching valve VB is set 2
Process the water pipe arrangement of discharging and the pipe arrangement interflow of processing water from the lower cavity 30c discharge second of husky filtration unit 30B from the lower cavity 30c of husky filtration unit 30A with second, be connected with the inlet portion of processing tank 15.And, in husky filtration unit 30A, the 30B pipe arrangement that the second processing water is discharged separately, sandwiched switching valve VA 3, switching valve VB 3
At switching valve VA 2The pipe arrangement of upstream side in be provided with tapping point, connect water shoot, constituting can be via switching valve VA 4Discharge cleaning draining 26 to the sea.Equally at switching valve VB 2The pipe arrangement of upstream side be provided with tapping point, connect water shoot, constituting can be via switching valve VB 4Discharge cleaning draining 26 to the sea.
In addition, at switching valve VA 3The pipe arrangement of upstream side tapping point is set, connect water shoot, constituting can be via switching valve VA 5Discharge cleaning draining 27 to the sea.Equally at switching valve VB 3The pipe arrangement of upstream side tapping point is set, connect water shoot, constituting can be via switching valve VB 5Discharge cleaning draining 27 to the sea.
In addition, towards supply pump P3, supply is temporarily stored in the second processing water of processing tank 15 from the export department that processes tank 15.
Switching valve VA 1～VA 5, VB 1～VB 5Be the switch-valve that is used under the random order in the state of basically full cut-off, standard-sized sheet, also namely carried out such as magnetic valve, motorized valve or air pressure valve etc. of open and close controlling by above-mentioned switching control 31.
(polyose absorbing treatment device 16)
Then, with reference to Fig. 1 the formation of polyose absorbing treatment device 16, particularly polyose sorbing material 16b are described in more detail.
In the present embodiment, among the composition (polyose composition) of the polyose in seawater within the contained organism, also particularly be conceived to the removal of TEP (Transparent Exopolymer Particles).TEP is that the corresponding molecular dimension of its molecular weight is the transparent grain shape organism of about 0.1 μ m～5 μ m.In the polyose composition, comprise in addition low-molecular polysaccharide about the less about 0.1 μ m of the corresponding molecular dimension of its molecular weight etc.Therefore, to have several nanometers to the absorption pore of the large-scale wide cut of hundreds of nanometers be effective to polyose sorbing material 16b.
Polyose absorbing treatment device 16 employed polyose sorbing material 16b as present embodiment use for example natural zeolite as described above.
Polyose absorbing treatment device 16, make the first composition of not removed fully by pretreating device 14 (polyose composition) of processing the water that flows into from lower cavity 16a, up-flow and pass through Adsorption in the layer of polyose sorbing material 16b, process water as second after processing afterwards and receive water to upper cavity 16c, send water to the upper cavity 30a of husky filtration unit 30.The size of the composition that polyose absorbing treatment device 16 wishs are removed for example be 1 μ m following about, particularly be dissolved in sugared composition in the seawater, specifically be to be effective as the outer particle (TEP) of a kind of hyaline cell of polyose etc. for absorption as the employed natural zeolite of polyose sorbing material 16b.
The employed natural zeolite of present embodiment is by SiO 270%, Al 2O 312%, Fe 2O 31.5%, the ratio of components of CaO3% etc. forms, and has mordenite and binds brilliant structure.Its particle diameter is 10～20mm.
In the first processing water of being processed by pretreating device 14, still contain the polyose composition in a large amount of seawater.There is boundary for the polyose adsorptive capacity that relies on polyose sorbing material 16b, even if make first to process under the overbottom pressure of water after passing through pretreating device 14 from the outlet pressure of filtration pump P2 through polyose absorbing treatment device 16, also can owing to continuous operation near the polyose saturated extent of adsorption, absorption property reduces thereupon.After being adsorbed onto the polyose saturated extent of adsorption, recover absorption property and be not easy, the top condition of setting the cleaning condition of regeneration (cleaning) time that comprises adsorption time (runtime) and polyose sorbing material 16b is important.
So, seawater desalination system 100A is by the polyose concentration (the second polyose concentration) of the second processing water after processing the polyose concentration (the first polyose concentration) of water and polyose sorbing material 16b and pass through by front first to the polyose sorbing material 16b of the polyose adsorptive capacity of polyose sorbing material 16b based on expression, set suitable cleaning condition, can in polyose absorbing treatment device 16, polyose be removed effectively.
In addition, the group that seawater desalination system 100A possesses a plurality of (in the present embodiment being 2) is connected in series polyose absorbing treatment device 16 and husky filtration unit 30, use polyose absorbing treatment device 16 of each group and the group of husky filtration unit 30 by switching, the seawater desalination is processed stopped just can to carry out specifically the not cleaning of the group of the polyose absorbing treatment device 16 of running and husky filtration unit 30.
Below, will use the path of polyose absorbing treatment device 16A and husky filtration unit 30A to be called the A of system, will use the path of polyose absorbing treatment device 16B and husky filtration unit 30B to be called the B of system.
(husky filtration unit 30)
The polyose sorbing material 16b that polyose absorbing treatment device 16 is contained is because first process flowing of water and so that the mineral bonding force reduces, sometimes follow simultaneously in second together with sugar or TEP composition as extremely fine particle and process flowing of water.Husky filtration unit 30 (being expressed as 30A, 30B among Fig. 1) is arranged to, and impact of flowing polyose sorbing material 16b out from polyose absorbing treatment device 16 as described above can not relate to reverse osmosis membrane type seawater desalination device 18.
(switching control 31)
Then, the function of switching control 31 described.Switching control 31 has not shown control part, can be connected with water analysis outfit 17, cleaning condition calculation apparatus 171A, rinse water heating unit 190A with communicating.And, carry out switching valve VA 1～VA 5, VB 1～VB 5Switching switch, so that will through the predefined time for example 12 hours from first processing after water processes the polyose absorbing treatment device 16 of a side system, husky filtration unit 30 that pretreating device 14 is supplied with, carry out the cleaning of this system, in the polyose absorbing treatment device 16 of the opposing party's system, husky filtration unit 30, process first during this period and process water.
The control part of switching control 31 is obtained switching valve VA 1～VA 5, VB 1～VB 5The open and-shut mode signal.In addition, the control part of switching control 31 carries out switching valve VA 1～VA 5, VB 1～VB 5Open and close controlling, carry out switching with respect to the supply of processing water from first of pretreating device 14 of the A of system and the B of system.In addition, switching control 31 is according to switching valve VA 1～VA 3, VB 1～VB 3Open and-shut mode judge and now just carrying out the polyose absorbing treatment device 16 of polyose adsorption treatment, the system of husky filtration unit 30 among two systems of A system and B system, in water analysis outfit 17, carry out the switching of the sampling pipe arrangement 160A/160B that obtains sample water in the water analysis outfit 17, the switching of sampling pipe arrangement 162A/162B.For this reason, the control device of switching control 31 sends switching signal to water analysis outfit 17.
And then, the control part of switching control 31 carries out the switching of the rinse water supplying tubing 191A/191B among rinse water supply device 19 and the rinse water heating unit 190A, the switching of 192A/192B (the polyose absorbing treatment device 16A/16B of the supply point of destination of rinse water, the switching of husky filtration unit 30A/30B).For this reason, the cleaning that the control device of switching control 31 receives cleaning condition calculation apparatus 171A begins, cleans the instruction signal that finishes, and sends switching signal to rinse water heating unit 190A.
For example, switching control 31 is by switching valve VA 1～VA 5, VB 1～VB 5Open and close controlling, the supply of carrying out processing for the seawater desalination of the A of system and the B of system water is switched.At this moment, switching control 31 carries out in the A of system in the situation of seawater desalination processing, with switching valve VA 1～VA 3Open, and close switching valve VB 1, VA 4, VA 5In the B of system, carry out in the situation of seawater desalination processing, with switching valve VB 1～VB 3Open, and close switching valve VA 1, VB 4, VB 5
In addition, switching control 31 in the situation of the cleaning of carrying out polyose absorbing treatment device 16A and husky filtration unit 30A, is closed switching valve VA 1～VA 3, and open switching valve VA 4, VA 5Thus, supply with rinse water via rinse water supplying tubing 191A to polyose absorbing treatment device 16A, supply with rinse water via rinse water supplying tubing 192A to husky filtration unit 30A, clean thus, and discharge the cleaning draining 26,27 after cleaning.In the situation of the cleaning of carrying out polyose absorbing treatment device 16B and husky filtration unit 30B, close switching valve VB 1～VB 3, and open switching valve VB 4, VB 5Thus, supply with rinse water via rinse water supplying tubing 191B to polyose absorbing treatment device 16B, supply with rinse water via rinse water supplying tubing 192B to husky filtration unit 30B, clean thus, and discharge the cleaning draining 26,27 after cleaning.
(water analysis outfit 17)
Then, the function of water analysis device described.Water analysis outfit 17 is analyzed the first and second polyose concentration and TEP concentration of processing in the water.For this reason, constitute the not shown polyose concentration analysis device, TEP concentration analysis device, a plurality of T-valve that are for example carried out action control by above-mentioned control part that comprises control part, is used for extracting from sampling pipe arrangement 122,160A, 160B, 162A, 162B sampling water.
More particularly, first part of processing water that water analysis outfit 17 will be processed by pretreating device 14 as water quality analysis with sample water 122A (() in, representing among Fig. 1), by from switching valve VA 1, VB 1Upstream side pipe arrangement branch sampling pipe arrangement 122 and obtain via the not shown T-valve of the action control of the control part that is subject to water analysis outfit 17.
Equally, second part of processing water that water analysis outfit 17 will be processed by polyose absorbing treatment device 16A, 16B as water quality analysis with sample water 162Aa, 162Ba (it is interior to be illustrated in () among Fig. 1), by from switching valve VA 2, VB 2 Sampling pipe arrangement 162A, the 162B of pipe arrangement branch of downstream side, obtain via the not shown T-valve that is carried out action control by the control part of water analysis outfit 17.
In addition, second part of processing water that will be processed by husky filtration unit 30A, 30B of water analysis outfit 17 as water quality analysis with sample water 160Aa, 160Ba (it is interior to be illustrated in () among Fig. 1), by switching valve VA 3, VB 3 Sampling pipe arrangement 160A, the 160B of pipe arrangement branch of upstream side, obtain via the not shown T-valve that is carried out action control by the control part of water analysis outfit 17.
And, water analysis outfit 17 is frequency, per 1 hour 1 time frequency for example in accordance with regulations, collect water quality analysis with water quality analysis sample water 160Aa, the 162Aa (perhaps 160Ba, 162Ba) of the system in the running within sample water 122a and the A of system and the B of system via above-mentioned T-valve, their contained polyose concentration and TEP concentration are analyzed.
In addition, in Fig. 1, omitted the pipe arrangement from the outlet side of the sampling pipe arrangement 122 in the water analysis outfit 17,160A, 160B, 162A, 162B, but they can be emitted to the sea also.In addition, the outlet pipe arrangement of sampling pipe arrangement 122,160A, 160B, 162A, 162B also can turn back to the positive downstream side of the pipe arrangement that branches out as the sampling pipe arrangement.
In any case, sampling pipe arrangement 122,160A, 160B, 162A, 162B, usually except with the A of system, B among second part of processing water of the system that stops in order to clean extract the relevant formation, all be in all the time water flowing state.And, in water analysis outfit 17, by predefined regulated procedure control, for example via T-valve (not shown) timefrequency in accordance with regulations, roughly side by side (need not the strict while, obtain the required time of sample water of specified amount from 2 pipe arrangements 122,160 of respectively taking a sample for analysis described later (system side of just processing the first processing water among sampling pipe arrangement 160A, the 160B), 162 (system side of just processing the first processing water among sampling pipe arrangement 162A, the 162B) and stagger) to obtain to sampling receptacle.Whether make above-mentioned sampling pipe arrangement 160A/160B arbitrarily T-valve action separately be used for sample water and obtain, whether make above-mentioned sampling pipe arrangement 162A/162B arbitrarily T-valve action separately to be used for that sample water obtains, namely which side system among A system and the B system is processing the first judgement of processing water, be based on and send to from switching control 31 that the switching signal of water analysis outfit 17 carries out.
Mention that at will the analysis in the water analysis outfit 17 is batch treatment.The quantitative analysis of the polyose concentration of the sample water of dependence water analysis outfit 17 is undertaken by phthalein sulfuric acid phenol method or high-speed liquid chromatography.For the quantitative analysis of the polyose concentration that relies on phthalein sulfuric acid phenol method, with glycogen as reference material.In addition, rely on the quantitative analysis of the TEP concentration of water analysis outfit 17 to be undertaken by alcian blue dyeing determination of absorbance.Rely on the analytical results 172 of water analysis outfit 17 to be exported to cleaning condition calculation apparatus 171A.
(cleaning condition calculation apparatus 171A)
Then, the function of cleaning condition calculation apparatus 171A described.In cleaning condition calculation apparatus 171A, has following functions: just input the analytical results 172 that is obtained by water analysis outfit 17 every the specified time, polyose sorbing material 16b in each system of A, B is replaced by new sorbing material TEP concentration ratio described later (polyose concentration ratio) C/C afterwards 0The resume data of value and the resume that clean employed cleaning model described later carry out record.
In addition, cleaning condition calculation apparatus 171A can register the cleaning condition for a plurality of cleaning models in advance of polyose absorbing treatment device 16 and husky filtration unit 30 in advance.
And cleaning condition calculation apparatus 171A is in the situation of the clear instruction that receives this system from switching control 31, based on the TEP concentration ratio C/C before just will switching 0, select suitable cleaning model from a plurality of cleaning model of in advance registration, to rinse water supply device 19 and rinse water heating unit 190A output purge signal 170A.Said cleaning condition, for example, made up the parameter of cleaning flow, the scavenging period of the time per unit of the rinse water that necessary required flow rate calculates, the temperature of rinse water etc. according to the husky filtering material for the polyose sorbing material 16b of polyose absorbing treatment device 16 and husky filtration unit 30.In cleaning condition calculation apparatus 171A, be registered with in advance a plurality of cleaning models that the parameter of these cleaning conditions is suitably changed and makes up, select one of them, the purge signal 170A corresponding with selected cleaning model sent to rinse water supply device 19 and rinse water heating unit 190A.
Details is in rear narration, in cleaning condition calculation apparatus 171A, is registered with as described above a plurality of cleaning model that size according to cleaning force has sorted, and sets for from the little cleaning model of cleaning force and selects in order.Cleaning condition calculation apparatus 171A, in situation about receiving from the clear instruction signal of switching control 31, the first up-to-date TEP concentration ratio C/C that processes before and after the processing of water that obtains when the polyose absorbing treatment device 16 of cleaning object 0For below the predefined threshold value, for example 0.2 when following, select and last time identical cleaning model.And, cleaning condition calculation apparatus 171A, the first up-to-date TEP concentration ratio C/C that processes before and after the processing of water that obtains at the polyose absorbing treatment device 16 of cleaning object 0When surpassing predefined threshold value, select the cleaning force ratio large cleaning model of cleaning model last time.The cleaning condition of the cleaning model that said cleaning force is large is such as the longer condition of the more condition of the flow of the time per unit that rinse water is arranged, scavenging period, condition that the rinse water temperature is higher etc.
(rinse water supply device 19)
Then, the function of rinse water supply device 19 described.Rinse water supply device 19, based on the purge signal 170A from cleaning condition calculation apparatus 171A, supply with rinse water according to flow, the scavenging period of the time per unit of the rinse water among the cleaning condition of being set by purge signal 170A to rinse water heating unit 190A.For this reason, though rinse water supply device 19 omits diagram, comprising: control part and from the pipe arrangement of processing tank 15 water intakings, the rinse water of fetching water is carried out the rinse water supply pump of force feed and flow rate regulating valve, flow sensor.
The control part of rinse water supply device 19, the speed of rotation of control rinse water supply pump and the aperture of flow rate regulating valve are so that the flow that is detected by flow sensor becomes the required flow that purge signal 170A indicates.
(rinse water heating unit 190A)
Then, the function of rinse water heating unit 190A described.Though rinse water heating unit 190A omits diagram, comprising: control part; Detect the temperature sensor of heater outlet water temperature; To supplying with for example electric heater that next rinse water heats from rinse water supply device 19; Supply with the not shown switching valve of rinse water via rinse water supplying tubing 191A or 191B and rinse water supplying tubing 192A or the corresponding pipe arrangement of 192B for the side in the B system of the A system of the polyose absorbing treatment device 16A of cleaning object and husky filtration unit 30 and polyose absorbing treatment device 16B and husky filtration unit 30B.
The control of the control part of rinse water heating unit 190A relies on the heat that adds of well heater, so that the temperature of rinse water becomes indicated temperature required of purge signal 170A.
Rinse water supply device 19, based on from the purge signal 170A of cleaning condition calculation apparatus 171A to polyose absorbing treatment device 16, when husky filtration unit 30 is supplied with heated wash water, rinse water heating unit 190A, with the cleaning condition that is suitable for being set by purge signal 170A for example the mode of flow, scavenging period, the rinse water temperature of the time per unit of rinse water be heated to rinse water temperature required and supply with.And rinse water heating unit 190A also supplies with to polyose absorbing treatment device 16 and husky filtration unit 30 except supplying with the next rinse water heating from rinse water supply device 19.On the other hand, in the situation of the rinse water of polyose absorbing treatment device 16 and husky filtration unit 30 being supplied with the normal temperature that heats, do not utilize the heating of rinse water heating unit 190A, directly rinse water is supplied to polyose absorbing treatment device 16 and husky filtration unit 30.
At this, rinse water supply device 19, switching control 31, rinse water heating unit 190A, rinse water supplying tubing 191A, 191B, 192A, 192B, switching valve VA 1～VA 5, VB 1～VB 5Consist of " wiper mechanism " that claims are put down in writing.
In addition, as the rinse water of supplying with from rinse water supply device 19, do not get final product so long as do not comprise the fluid of TEP, for example can remove the processing tank 15 that second of TEP processes water from temporarily storing as described above, process water with second and carry out, can also use in addition the concentrated draining 24 of discharging from reverse osmosis membrane type seawater desalination device 18.Below, to use the second situation of processing water of processing tank 15 to describe as example as processing water.
Certainly, can use the water of the water-supply line of the fresh water 20 that obtains from reverse osmosis membrane type seawater desalination device 18 or other system, but use the fresh water 20 that obtains from reverse osmosis membrane type seawater desalination device 18, can cause the formation efficiency of fresh water 20 of the 100A of seawater desalination system to reduce.
Because the characterization of adsorption that depends on natural zeolite of TEP mainly is physical adsorption, so, need not and to form extra high temperature for the rinse water from polyose sorbing material 16b desorb TEP, but it is high to have adsorbed the possibility of the such low-molecular polysaccharide class less than TEP molecular dimension etc. together with TEP in polyose sorbing material 16b.For this reason, except the desorb of TEP, also need such low-molecular polysaccharide composition is carried out desorb, for this reason also need to be by rinse water heating unit 190A heated wash water.The low-molecular polysaccharide class is easily dissolving or viscosity reduction in high-temperature water, can break away from from the natural zeolite as polyose sorbing material 16b.
In addition, in the present embodiment, rinse water supply device 19, rinse water heating unit 190A supply with rinse water and carry out the cleaning of polyose absorbing treatment device 16, also husky filtration unit 30 are supplied with rinse water and are carried out the cleaning of husky filtration unit 30 simultaneously.
This is because also adsorbed TEP or low-molecular polysaccharide class etc. in flowing out to the polyose sorbing material 16b of husky filtration unit 30, so make its desorb.
(reverse osmosis membrane type seawater desalination device 18)
Reverse osmosis membrane type seawater desalination device 18 uses reverse osmosis membrane with the seawater desalination.Temporarily being stored in the second processing water of processing tank 15 is supplied to reverse osmosis membrane type seawater desalination device 18 via supply pump P3, high-pressure pump P4.Be fed into second in the reverse osmosis membrane type seawater desalination device 18 and process water by reverse osmosis membrane filtration, be separated into concentrated draining 24 and fresh water 20.Fresh water 20 is transferred to not shown aqua storage tank etc., is used for various uses.Concentrated draining 24 turns back to marine.
In addition, only showing typically a reverse osmosis membrane type seawater desalination device 18 in Fig. 1, but a plurality of reverse osmosis membrane type seawater desalination devices 18 also can be set in parallel, also can in series arrange many in addition, can also be their both sides' combination.
(purging method of polyose sorbing material)
The detailed situation of the purging method of the polyose sorbing material among the seawater desalination system 100A then, is described with reference to Fig. 2 to Fig. 4.As described above, in seawater desalination system 100A, for supply with the first next processing water from pretreating device 14, switching control 31 is at the polyose absorbing treatment device that makes a side after 16 non-stop run specified times, switch the first current of processing water to the opposing party's polyose absorbing treatment device 16, carry out the cleaning after a side the work of polyose absorbing treatment device 16.At this moment, cleaning condition calculation apparatus 171A, the TEP concentration of sending from water analysis outfit 17 of for example processing before and after the processing of water based on first of the polyose absorbing treatment device 16 that relies on a side obtains the TEP concentration ratio, recently determining whether based on this TEP concentration needs to clean, determining in the situation of need cleaning, selecting this cleaning model among these a plurality of cleaning models.
At this, said TEP concentration ratio is the value of calculating by following formula (1) in water analysis outfit 17, is the variable indicator that relies on the TEP adsorption rate of polyose absorbing treatment device 16.Why using the TEP concentration ratio to carry out the evaluation of TEP adsorption rate, is because constantly all changing as the TEP concentration in the seawater of processed water.
In addition, the TEP concentration of present embodiment shown in Figure 4 is the parameter of xanthan gum having been carried out quantification as reference material.
TEP concentration ratio C/C 0=(the water quality analysis TEP concentration measurement of sample water 162a)/(the water quality analysis TEP concentration measurement of sample water 122a) ... (1)
At this, the water quality analysis sample water 162Aa of water quality analysis in the sample water 162a presentation graphs 1, any one party of 162Ba.At this, " water quality analysis with the TEP concentration measurement of sample water 122a " is corresponding with " the first polyose concentration " that claims are put down in writing, and " water quality analysis with the TEP concentration measurement of sample water 162a " is corresponding with " the second polyose concentration " that claims are put down in writing.
In addition, rely on the TEP clearance of polyose absorbing treatment device 16 to calculate by following formula (2).
TEP clearance={ (the water quality analysis TEP concentration of sample water 122a)-(the water quality analysis TEP concentration of sample water 162a) } * 100/ (water quality analysis TEP concentration of sample water 122a) ... (2)
In the present embodiment, with TEP concentration ratio C/C 0=0.2 is made as threshold value.This threshold value is not to make the pollution development of reverse osmosis membrane of reverse osmosis membrane type seawater desalination device 18 or the degree that the performance of reverse osmosis membrane is reduced, and refers to allow to continue carry out the scope of the polyose adsorption treatment of same system.
Fig. 2 be the processing water yield in the expression polyose absorbing treatment device 16 and process after the second graphic representation of processing the relation of the TEP concentration in the water.Fig. 3 is the cleaning model of expression experimental result and the TEP concentration ratio C/C at circulation end 0The graphic representation of variation.In Fig. 2, transverse axis represents the processing water yield (L: rise) in the polyose absorbing treatment device 16.At this, with after the replacing filling of the new polyose sorbing material 16b in the polyose absorbing treatment device 16 from use begin till the initial clean first process water processing during be called the 1st circulation, then, will finish from the cleaning of going ahead of the rest till the ensuing cleaning first process water processing during be called the 2nd, 3,4..., (N-1), N, (N+1) circulation.Fig. 2 is at the example of having striden in per 1 situation of 12 hours having processed the first processing water that circulates.The longitudinal axis of Fig. 2 is before and after being processed by the dependence polyose absorbing treatment device 16 that above-mentioned formula (1) is calculated, namely second processes water and the first TEP concentration ratio C/C that processes in the water 0
In Fig. 2, the adsorption treatment of a polyose absorbing treatment device 16 carry out continuously per 1 the circulation 12 hours after, by rinse water natural zeolite is cleaned to regenerate.The result that Fig. 2 extracts the 1st circulation, (N-1) circulation, N circulation, (N+1) circulation represents.Among each result, the processing water yield of the starting point of each circulation is the value at 0 some place, molecule denominator with above-mentioned formula (1) consists of the TEP concentration of using sample water 122a from the water quality analysis of pretreating device 14, becomes the state of the adsorption treatment that relies on polyose absorbing treatment device 16.Therefore, the value at the initial stage of each circulation is 1.0.
Experimental result according to the inventor, from the 1st circulation (representing with " ◇ " mark Fig. 2) until (N-1) circulation (representing with " " mark among Fig. 2), continue to have carried out to rely on 10 minutes the clean (being made as the cleaning model 1 of Fig. 3) of 20 ℃ normal-temperature water.As shown in Figure 2, from the 1st circulation until (N-1) circulates the TEP concentration ratio C/C during each loop ends 0For surpassing 0.2 scope.For this reason, the cleaning during each loop ends continues to carry out by identical conditions (cleaning model 1).But, for N circulation (representing with " △ " mark among Fig. 2), in the way of circulation, TEP concentration ratio C/C 0Surpassed 0.2.For this reason, for the cleaning after the N loop ends, carry out cleaning condition (cleaning model 1) till current to the switching of the cleaning model 2 with the higher cleaning condition of cleaning force.
In situation shown in Figure 2, for the cleaning after the N circulation, carried out relying on 10 minutes clean of 50 ℃ heating water as cleaning model 2.Its result, the TEP concentration ratio C/C when (N+1) circulation (representing with " zero " mark among Fig. 2) finishes 0Again be lower than 0.2.Though not shown, for the cleaning of (N+2) circulation, do not change cleaning model, continue to carry out the cleaning under the cleaning model 2, but the absorption property of natural zeolite kept, namely C/C 0＜0.2.
In addition, though Fig. 2 is not shown, confirmed that the cleaning model when (N+1) loop ends turns back in the situation of cleaning model 1, the TEP concentration ratio C/C in (N+2) circulation 0Surpass 0.2.
Fig. 3 is the cleaning model of expression experimental result and the TEP concentration ratio C/C at circulation end 0The graphic representation of variation.The experimental result of Fig. 3 is the event result that is different from experiment shown in Figure 2.In Fig. 3, transverse axis represents the cycle number of the absorption/clean of polyose absorbing treatment device 16, and second the when longitudinal axis is each loop ends processed the TEP concentration ratio C/C of water 0In Fig. 3, (the 1st circulation) is until the N-1 circulation (during 1) from adsorption treatment, according to cleaning model 1 (relying on 10 minutes clean of 20 ℃ normal-temperature water), from N circulation until (P-1) circulation (during 2), according to cleaning model 2 (relying on 5 minutes clean of 50 ℃ heating water), from P circulation until the Q-1 circulation (during 3), according to cleaning model 3 (relying on 5 minutes clean of 80 ℃ heating water), be recycled to R-1 circulation (during 4) from Q, according to cleaning model 4 (relying on 5 minutes clean of 99 ℃ heating water), carry out respectively clean.
In addition, what use in cleaning model 4 is 99 ℃ hot water, even but 90 ℃ hot water also can obtain the cleaning performance of roughly the same degree.1 is corresponding during among Fig. 2 the 1st circulation the～the N-1 circulation and Fig. 3.In addition, the N among Fig. 2 circulation and N+1 circulation be contained in Fig. 3 during 2.
At this, the flow velocity of the rinse water in the experimental result shown in Figure 3 is described.Parameter value as the adsorption operations that represents the dependence sorbing material uses air speed (SV:Space Velocity) usually.Air speed SV is with processing water flow velocity (unit: m 3/ h) divided by sorbing material volume (m 3) value that obtains, the unit of SV becomes (h -1).In addition, air speed SV also is with processing waterline speed (LV:Linear Velocity, unit: the value that m/h) obtains divided by the length (m) of the flow direction of the processing water in the adsorption layer.
In common water treatment system, mostly be 10 (h with respect to the SV value of the pre-treatment of reverse osmosis membrane -1) below, SV=4～5.In the present embodiment, the SV value of the processing water in the polyose absorbing treatment device 16 is 10 (h -1).In addition, for clean, because the flow velocity of rinse water is larger on the cleaning performance impact, so, usually strengthen air speed SV and implement to clean.In the present embodiment, the SV value of the rinse water in the polyose absorbing treatment device 16 is 300 (h -1).The flow velocity of rinse water is not limited to above-mentioned value, but because the difference of the flow velocity of rinse water and produce more or less difference at the reprocessing cycle number.
As shown in Figure 3, in the 1 N-1 circulation that comprises, the analytical results of water analysis outfit 17 becomes C/C during the cleaning that relies on cleaning model 1 0＞0.2.For this reason, cleaning condition calculation apparatus 171A is judged as and need to makes cleaning model 1 further High Level (switching to cleaning model 2), rinse water supply device 19 and rinse water heating unit 190A outputting cutting is changed into the purge signal 170A of cleaning model 2.
Later on too, in the 2 P-1 circulations that comprise, the analytical results of water analysis outfit 17 becomes C/C during the cleaning that relies on cleaning model 2 0＞0.2.For this reason, cleaning condition calculation apparatus 171A is judged as and need to makes cleaning model 2 further High Levels (switching to cleaning model 3), rinse water supply device 19 and rinse water heating unit 190A outputting cutting is changed into the purge signal 170A of cleaning model 3.In addition, in the 3 Q-1 circulations that comprise, the analytical results of water analysis outfit 17 becomes C/C during the cleaning that relies on cleaning model 3 0＞0.2.For this reason, cleaning condition calculation apparatus 171A is judged as and need to makes cleaning model 1 further High Level (switching to cleaning model 4), rinse water supply device 19 and rinse water heating unit 190A outputting cutting is changed into the purge signal 170A of cleaning model 4.
In addition, during 2 and during in 3, beyond above-mentioned P-1 circulation and Q-1 circulation, also have C/C 0(X1～X5), still, not switching cleaning model in this moment is in order to lengthen between the usage period of polyose absorbing treatment device 16 by identical cleaning model is continued at＞0.2 position.For example, become C/C for X1 0＞0.2, but in ensuing circulation, become C/C 0＜0.2, also can carry out the interior cleaning of specialized range even if continue as can be known cleaning model 2.
At will mention, as described above, cleaning condition calculation apparatus 171A has following functions: for polyose absorbing treatment device 16A, 16B, husky filtration unit 30A, 30B, be to have carried out such resume according to which cleaning model among the predefined cleaning model to carry out pre-recorded to the cleaning of each time.
Therefore, also can not that analytical results at water analysis outfit 17 becomes C/C 0Just switch immediately cleaning model after＞0.2, but after cleaning at C/C 0Switch again cleaning model behind＞0.2 the state continuance stipulated number.
In addition, the cleaning condition of the cleaning condition of polyose absorbing treatment device 16 and husky filtration unit 30 need not identical.In this case, 2 electric heaters that in rinse water heating unit 190A, possess polyose absorbing treatment device 16 usefulness and husky filtration unit 30 usefulness, in addition, mode with the flow of the time per unit that can set respectively rinse water separately possesses flow rate regulating valve, and the mode of perhaps controlling with the time that separately rinse water is flowed possesses other switching valve.And cleaning condition calculation apparatus 171A is input to rinse water supply device 19, rinse water heating unit 190A with the purge signal 170A that has comprised respectively the cleaning condition of the cleaning condition of polyose absorbing treatment device 16 and husky filtration unit 30.
Fig. 4 is the graphic representation that represents to rely on the organic change in concentration before and after the adsorption treatment of polyose absorbing treatment device 16 according to material.In Fig. 4, transverse axis is the processing water yield (L: rise) in the polyose absorbing treatment device 16, and left end represents to process water yield 0L, more turns right and processes the water yield just more for increasing.In Fig. 4, the longitudinal axis represents to process the organic substance concentration in the water, and the left longitudinal axis of the graphic representation of Fig. 4 represents TEP concentration, and the right longitudinal axis of the graphic representation of Fig. 4 represents complete sugared concentration.The line that mark " ◇ " mark represents among the figure, namely TEP concentration is that xanthan gum is carried out the parameter that quantification represents as reference material, its unit is mg-Xeq/L.At this, [X] among " Xeq " refers to xanthan gum, and " eq " is the meaning of suitable (equivalent), namely with the suitable contracted notation of " Xeq " expression xanthan gum.
Complete sugared concentration, be that uronic acid concentration (line that mark " " mark represents among the figure) and neutral sugar concentration (line that mark " △ " mark represents among the figure) are carried out the parameter that quantification represents as reference material, its unit is mg-Geq/L.At this, " G " among " Geq " refers to glycogen, and " eq " is the meaning of suitable (equivalent), namely with the suitable contracted notation of " Geq " expression glycogen.
As shown in Figure 4, each in TEP and full sugar all confirmed to rely on the adsorption effect of natural zeolite.Although can't carry out the analytical results of TEP concentration and complete sugared concentration numeric ratio, the words of size, the speed than TEP change in concentration when the reduction of complete sugared concentration is larger, have the easier tendency of being adsorbed by natural zeolite of complete sugared composition.
State to TEP and the full minimizing of sugar compares in detail, is described as follows.The composition of TEP mainly is made of acid mucopolysaccharides, thinks that the size of material is approximately several microns to the particulate material of the size of submicron.On the other hand, the composition of full sugar refers to by molecular dimension from several microns until total amount of organic the minimum monose molecule 1kDa (molecular weight 1000) below, the seawater that does not comprise albumen or amino acids that has nothing to do with size.Complete sugared concentration utilizes phthalein sulfuric acid phenol absorbance method to measure, and measures according to the both sides' of wavelength 480nm and 490nm absorbancy.Think that the absorbance of 480nm also represents the concentration of uronic acid among complete sugared concentration.In addition, the absorbance of 490nm also represents the concentration of neutral sugar among complete sugared concentration, comprise the sugar that molecular weight is little.Thus, for the absorption that relies on natural zeolite, think and adsorb at first easily the little sugar of molecular weight, then adsorb molecular weight large near granular TEP.
In addition, in the present embodiment, though do not carry out the explanation of the cleaning condition of cleaning model more than 4, can realize fully the further High Level of cleaning condition.As an example, for example also can be " 10 minutes the clean that relies on 99 ℃ hot water ", " 100 ℃ steam flushing ".
(effect)
According to present embodiment, by the TEP concentration ratio C/C before and after the processing of being calculated polyose absorbing treatment device 16 by water analysis outfit 17 0, can judge easily the degree that the adsorption concentration of the polyose sorbing material 16b of polyose absorbing treatment device 16 reduces.In addition, in cleaning condition calculation apparatus 171A, whether record the resume that polyose absorbing treatment device 16A, 16B, husky filtration unit 30A, 30B have been carried out cleaning last time with the cleaning model of predefined cleaning model etc., according to the rules near the TEP concentration ratio C/C moment of finishing of first of the time the processing of processing water 0The result, automatically whether decision is used and last time identical cleaning model, and then whether uses the high cleaning model of cleaning force.Its result bring burden can not for running person, can avoid in addition originally need not making rinse water to become that the water of high temperature is more but selected the cleaning model of the water of high temperature more and situation that the operating cost of seawater desalination system 100A is increased.
In addition, keep owing to during can the span length adsorptive power of the polyose sorbing material 16b of polyose absorbing treatment device 16 be regenerated, so, the polyose sorbing material 16b that can reduce mineral is the replacement frequency of natural zeolite, also can reduce the operating cost of seawater desalination system 100A from this meaning.
In the patent documentation 1,2 of conventional art, put down in writing the example that uses ultra-filtration membrane (UF film) at pretreating device, can divide with dirty matter and filter the large polyose of molecular weight or organism.But, in the situation of the tamper that removes the UF film that is formed by these materials by back washing, when using the high condensed water of the salt concentration of discharging from reverse osmosis membrane type seawater desalination device, there is the scale composition, in the cleaning of the medicine that has used clorox or alkali etc., can be with organic matter removal, but as its side effect, have the scale composition of calcium carbonate or Losantin to be attached to the UF film.As its resolution policy, add sour water and become to remove in order to the scale that will produce.Namely, for the technology that patent documentation 1,2 is put down in writing, owing in rinse water, also use alkaline agent and these two kinds of medicaments of acid, this waste liquid directly can't be carried out draining to the sea, need to be in the draining enforcement purifying treatment that takes a step forward, the operating cost of seawater desalination system increases.
In addition, in the technology that patent documentation 2 is put down in writing, put down in writing: the countermeasure as during the circulation of prolongation UF membrane washing, rinse water is heated, enumerate cleaning performance.
But, in the present embodiment, main dirty matter part, the large polyose of adsorb organic compound or molecular weight in polyose absorbing treatment device 16 of filtering in pretreating device 14.And the cleaning of polyose absorbing treatment device 16 is also used from the concentrated draining 24 of the second processing water or 18 discharges of reverse osmosis membrane type seawater desalination device.Therefore, do not comprise polyose, can be easily from polyose sorbing material 16b with the polyose desorb.Even if it is marine to comprise that the cleaning draining 26,27 of the polyose that is desorbed directly is discharged to, because the polyose that is desorbed from polyose sorbing material 16b is the material that originally just is included in the seawater, so directly no problem to extra large draining.
In addition, in the present embodiment, as the full concentration of saccharide ratio that passes through the processing water of front and back at polyose absorbing treatment device 16, with TEP concentration ratio C/C 0Defined by above-mentioned (1) formula, but be not limited thereto, also can use the quantitative analysis results of the polyose concentration of the dependence phthalein sulfuric acid phenol method that in water analysis outfit 17, obtains.
In addition, as the sampling water of the processing of second after passing through at polyose absorbing treatment device 16 water, also can substitute the sampling water that uses sampling pipe arrangement 160A/160B, but adopt the sampling water of sampling pipe arrangement 162A/162B.
And then, in the present embodiment, use polyose sorbing material 16b as mineral in polyose absorbing treatment device 16 has adopted the experimental result of natural zeolite to be illustrated, but the polyose sorbing material 16b of mineral is not limited to natural zeolite, can use synthetic zeolite, activated alumina, silica gel, Porous clay mineral, clay intercalation compound etc.The polyose sorbing material is owing to have several nanometers to the absorption pore of the large-scale wide cut of hundreds of nanometers, so be effective to the absorption of polyose.
For example, above-mentioned clay intercalation compound is the material that is contained in a large number in the soil, and existing maximum is aluminium silicate mineral.The clay intercalation compound illustrates the grid system of stratiform as microstructure.The trellised element of structure is limited to O, H, Si, Al, Fe, Mg, Li.Among them, Al, Fe, Mg, Li do not change crystal habit ground and mutually replace.
The stratiform grid consists of by the layer of 2 kinds.One is Si 2+Ion is by O -The silicic acid tetrahedrallayer that surrounds, another is Al 3+Ion is by 6 OH -Perhaps O 2-The octahedral layer that surrounds.The layer of this 2 kind consists of the basic structure of stratiform lattice type clay mineral (clay intercalation compound).Among the positively charged ion that consists of the stratiform grid, comprising Al 3+Or Fe 3+The cationic situation of 3 such valencys, comprise Mg +Or Fe 2+In the cationic situation of such divalent, because interfloor distance is different, so occur changing in characteristic.In addition, also become different types for the combination of the lamination state of tetrahedrallayer and octahedral layer different, claim to classify by exhaling of 1: 1 type mineral, 2: 1 type mineral, 2: 2 type mineral etc., and produce difference in the characteristic of ionic adsorption performance, positively charged ion replacing capacity etc.
In addition, in the present embodiment, rinse water supplying tubing 191A, 191B are connected with the lower cavity 16a of polyose absorbing treatment device 16A, 16B, comprise switching valve VA 4, VB 4Water shoot be connected with upper cavity 16c side, but be not limited thereto.Also can constitute, rinse water supplying tubing 191A, 191B are connected with the upper cavity 16c of polyose absorbing treatment device 16A, 16B, comprise switching valve VA 4, VB 4Water shoot be connected with lower cavity 16a side.
Equally, in the present embodiment, rinse water supplying tubing 192A, 192B are connected with the upper cavity 30a of husky filtration unit 30A, 30B, comprise switching valve VA 5, VB 5Water shoot be connected with lower cavity 30c side, but be not limited thereto.Also can constitute, rinse water supplying tubing 192A, 192B are connected with the lower cavity 30c of husky filtration unit 30A, 30B, comprise switching valve VA 4, VB 4Water shoot be connected with upper cavity 30a side.
Like this, by changing the connection of rinse water supplying tubing 191A, 191B, 192A, 192B and above-mentioned water shoot, polyose absorbing treatment device 16A, 16B and husky filtration unit 30A, 30B carry out back washing by rinse water, process the cleaning of the first direction following current of flowing when processing water with relying on of above-mentioned embodiment and compare, can improve cleaning efficiency.
For example, the layer of the polyose sorbing material 16b of natural zeolite is owing to make the first processing water adsorb the polyose composition from the process of lower cavity 16a up-flow, so, the natural zeolite of lower floor adsorbs the more polyose composition of volume, press following current moving phase ratio with rinse water, polyose composition in the desorb of adverse current time institute arrives lower cavity with short range, and the possibility that improves cleaning efficiency is high.Also can be described as same for husky filtration unit 30A, 30B.
In addition, in the present embodiment, among polyose absorbing treatment device 16A, husky filtration unit 30A and polyose absorbing treatment device 16B, husky filtration unit 30B that 2 systems of A, B system have, for example make A system running carry out first when carrying out the cleaning of this system after processing water in 12 hours, switching to the B system and the B system turned round 12 hours, but do not limiting.
Switching valve VA 1, VB 1Be not switch-valve, but can carry out the valve that flow is adjusted by the aperture adjustment, for example, also can be for cleaning the system A that finishes in above-mentioned example, switching control 31 is after cleaning end, with switching valve VA 1Be adjusted into the aperture of the minimum flow rate that flows through regulation, and switching valve VA 2, VA 3Be full-gear, in the A system, also flow through first and process water.Make first to process the flow that water flows through regulation by the system that is through with for cleaning like this, can among the polyose absorbing treatment device 16 of this system, husky filtration unit 30, suppress thin mattress propagation.
" modified example of the first embodiment "
Then, with reference to Fig. 5 the related seawater desalination system 100B of the modified example of the first embodiment is described.Fig. 5 is the summary pie graph of the related seawater desalination system 100B of the modified example of the first embodiment.
The point that the seawater desalination system 100B of this modified example is different from the seawater desalination system 100A of the first embodiment is mainly following 5 points: (1) rinse water supply device 19 is deleted, (2) cleaning condition calculation apparatus 171A replaces cleaning condition calculation apparatus (cleaning condition determination means) 171B, (3) rinse water heating unit 190A replaces hot blast control device 190B, (4) rinse water supplying tubing 191A, 191B, 192A, 192B is deleted, (5) polyose absorbing treatment device 16A, 16B and husky filtration unit 30A, 30B possesses device (the cleaning heating atmosphere feed unit 41A that is blown into hot blast or heating steam with the such inside that is formed in of stove, 41B, 44A, 44B).
Cleaning condition calculation apparatus 171B in this modified example is the function identical with cleaning condition calculation apparatus 171A basically, but in advance the cleaning model of cleaning condition of registration be the amount of being blown into (wind speed), air or the heating steam of air or heating steam temperature, add the combination of parameter of blowing time etc. of warm air or heating steam.In order to improve cleaning force, mainly lengthened the blowing time that adds warm air or heating steam that is used for improving temperature air or heating steam.
Cleaning condition calculation apparatus 171B will represent that the purge signal 170B of above-mentioned cleaning model sends to hot blast control device 190B.Hot blast control device 190B has omitted control signal wire in Fig. 5, it controls cleaning described later with heating atmosphere feed unit 41A, 41B, 44A, 44B.
By adding in the situation that warm air or heating steam cleans polyose absorbing treatment device 16 (being expressed as 16A, 16B among Fig. 5), husky filtration unit 30 (being expressed as 30A, 30B among Fig. 5), such as carrying out the form that heat-insulating mode forms stove with surrounding complete cycle with the container with stainless steel by refractory brick etc.And, supply with to the polyose sorbing material 16b of mineral or husky filtering material 30b by adding warm air or heating steam, the polyose sorbing material 16b of mineral or polyose composition evaporation that husky filtering material 30b adsorbs or thermolysis etc. are removed.
In Fig. 5, in polyose absorbing treatment device 16 (being expressed as 16A, 16B among Fig. 5), will clean with heating atmosphere feed unit 41 (being expressed as 41A, 41B among Fig. 5) and be arranged on lower cavity 16a so that supply adds warm air or heating steam.
Clean with heating atmosphere feed unit 41 and for example possess well heater and the gas blower that utilizes electric power or oil or burning of gas gas to heat, the air or the heating steam that have been blown into by heater heats from supplying opening 42 (being expressed as 42A, 42B Fig. 5) to polyose absorbing treatment device 16 by gas blower.Thus, the natural zeolites in the polyose absorbing treatment device 16 are heated, adsorbent (polyose composition) evaporation or thermolysis etc. and be desorbed.Be deflated from the venting port 43 (being expressed as 43A, 43B Fig. 5) of the upper cavity 16c side that is located at polyose absorbing treatment device 16 from add warm air or the heating steam of cleaning with 41 supplies of heating atmosphere feed unit.Mention that at will with heating in the atmosphere feed unit 41, be provided with the pipe arrangement of for example supplying with the upper water that is used for generating steam and the flow rate regulating valve of adjusting its flow in cleaning, its flow rate regulating valve is controlled by hot blast control device 190B, but omits in Fig. 5.
In addition, in Fig. 5, for husky filtration unit 30 (being expressed as 30A, 30B among Fig. 5) too, to clean with heating atmosphere feed unit 44 (being expressed as 44A, 44B among Fig. 5), supplying opening (being expressed as 45A, 45B among Fig. 5) and be arranged on upper cavity 30a side so that supply adds warm air or heating steam, venting port 46 (being expressed as 46A, 46B among Fig. 5) will be arranged on lower cavity 30c side.At venting port 46 places, the cut-off valve 47 (being expressed as 47A, 47B among Fig. 5) of watertight is set.
Lower cavity 16a side connection at polyose absorbing treatment device 16A comprises switching valve VA 4Water shoot, connect in the lower cavity 16a side of polyose absorbing treatment device 16B and to comprise switching valve VB 4Water shoot, opened and closed by switching control 31 control equally with the first embodiment.
Mention that at will in this modified example, cut-off valve 47 is is also opened and closed by switching control 31 controls.
By switching control 31, for example when the A system becomes the action of cleaning, switching control 31 is at first to the switching valve VB of B system 1～VB 3Open control, to the switching valve VA of A system 1～VA 3Close control, and to switching valve VA 4, VA 5Open control, in addition cut-off valve 47A is opened control.Like this, process water to the mobile B system side that switches to of A system with first, and with the processing water of polyose absorbing treatment device 16A, husky filtration unit 30A to extra large draining.In the stage that draining finishes, hot blast control device 190B will clean with heating atmosphere feed unit 41A, 44A and start, and clean with the cleaning model of the regulation corresponding with the purge signal 170B that sends instruction from cleaning condition calculation apparatus 171B.When the cleaning under the cleaning model of regulation finishes, hot blast control device 190B will clean with heating atmosphere feed unit 41A, 44A and stop.And, 31 couples of switching valve VA of switching control 4, VA 5Close control, 47A closes control to cut-off valve, makes the A system become holding state.
In addition, the cleaning condition of the cleaning condition of polyose absorbing treatment device 16 and husky filtration unit 30 needn't be identical.
At this, switching control 31, hot blast control device 190B, switching valve VA 1～VA 5, VB 1～VB 5, clean " wiper mechanism " put down in writing with formation claims such as heating atmosphere feed unit 41A, 41B, 44A, 44B.
At will mention, as an example of the cleaning model in the modified example of present embodiment, such as enumerating " 100 ℃ steam flushing ", " the heating air purge below 100～250 ℃ ", " 250～500 ℃ heating air purge " etc.Experimental result according to the inventor, particularly " 100 ℃ steam flushing " and " the heating air purge below 100～250 ℃ " are that effectively " 250～500 ℃ heating air purge " are effective to the disengaging of thermolysis resultant to the disengaging of the low-boiling-point organic compound of TEP etc.
In addition, in heating air purge or steam flushing, come self-stip to need not straight-through at polyose absorbing treatment device 16, husky filtration unit 30 and discharge from venting port with add warm air or the heating steam of heating atmosphere feed unit 41,44, major part is returned cleaned with heating atmosphere feed unit 41,44, form and only a part is discharged such circulating-heating mode, this is preferred at thermo-efficiency.
In addition, also can be in the first embodiment and then make up the modified example of the first embodiment.
" the second embodiment "
Then, with reference to Fig. 6 the second embodiment is described.
Fig. 6 is the summary pie graph of the related seawater desalination system 600 of the second embodiment.
In seawater desalination system 100A shown in Figure 1, used natural zeolite as the polyose sorbing material.Seawater desalination system 600 is gac as polyose sorbing material 57b use.
In Fig. 6, to the component part same with the related seawater desalination system 100A (with reference to Fig. 1) of the first embodiment, the mark Reference numeral identical with Fig. 1 and the repetitive description thereof will be omitted.
In seawater desalination system 600, substitute polyose absorbing treatment device 16 (being expressed as 16A, 16B among Fig. 1), be provided with the polyose absorbing treatment device 57 (in Fig. 6 be expressed as 57A, 57B) of gac use as polyose sorbing material 47b.Polyose absorbing treatment device 57 is same with polyose absorbing treatment device 16, adsorbs the namely polyose composition removal of composition (material) that will do not removed fully by pretreating device 14 by adsorption treatment.Gac is because to process the possibility that water flows out with first low, so, husky filtration unit 30 as shown in Figure 1 is not set in seawater desalination system 600.In seawater desalination system 600, also same with seawater desalination system 100A shown in Figure 1, the carbohydrate in the adsorbing seawater is TEP particularly, and the cleaning frequency of reverse osmosis membrane or replacement frequency are reduced.
At will mention, in polyose absorbing treatment device 57, in lower cavity 57a, import first and process water, up-flow in as the layer of the gac of polyose sorbing material 57b, received water towards upper cavity 57c, be temporarily stored in flowing process tank 15 at back segment.
At this, rinse water supply device 19, switching control 31, rinse water heating unit 190A, rinse water supplying tubing 191A, 191B, switching valve VA 1, VA 2, VA 4, VB 1, VB 2, VB 4Consisted of " wiper mechanism " that claims are put down in writing.
As described above, the seawater desalination system 600 related according to present embodiment, with the first embodiment equally based on cleaning up-to-date TEP concentration ratio C/C regularly 0(polyose concentration ratio) selects cleaning model.And, by the cleaning model of selecting the A system of cleaning object or the polyose absorbing treatment device 57 of the side in the B system are cleaned.Thus, the performance of the polyose sorbing material 57b of gac can be kept, the polyose in the seawater can be stably removed.In addition, the seawater desalination system 600 related according to present embodiment, by the polyose in the seawater is stably removed, the pollution that can reduce reverse osmosis membrane is biofouling namely, can reduce cleaning frequency or the replacement frequency of reverse osmosis membrane.And then the seawater desalination system 600 related according to present embodiment by reducing cleaning frequency or the replacement frequency of reverse osmosis membrane, can reduce the operating cost of seawater desalination system, but and then Reduction of the environment load.
In addition, as illustrating among the effect of the first embodiment, eliminate the problem of using the processing of the draining that produces in the situation of UF film in pre-treatment, can reduce the operating cost of seawater desalination system 600.
Description of reference numerals
100A, 100B, 600 seawater desalination systems
12 water intaking grooves
14 pretreating devices
15 process tank
16A, 16B polyose absorbing treatment device
16b polyose sorbing material
17 water analysis outfits (polyose concentration measuring mechanism)
18 reverse osmosis membrane type seawater desalination devices (reverse osmosis membrane processing device)
19 rinse water supply devices (wiper mechanism)
The husky filtration unit of 30A, 30B
31 switching controls (wiper mechanism)
41A, 41B, 44A, 44B clean with heating atmosphere feed unit (wiper mechanism)
57A, 57B polyose absorbing treatment device
57b polyose sorbing material
122,160A, 160B, 162A, the 162B pipe arrangement of taking a sample
171A, 171B cleaning condition calculation apparatus (cleaning condition determination means)
190A rinse water heating unit (wiper mechanism)
190B hot blast control device (wiper mechanism)
191A, 191B, 192A, 192B rinse water supplying tubing (wiper mechanism)
The SW seawater
VA 1～VA 5, VB 1～VB 5Switching valve (wiper mechanism).

Claims (5)

1. seawater desalination system that uses reverse osmosis membrane is characterized in that possessing:
Pretreating device, this pretreating device carries out pre-treatment to the seawater that water intaking obtains,
The polyose absorbing treatment device, this polyose absorbing treatment device uses the polyose sorbing material, and contained polyose composition in the first processing water that was undertaken by above-mentioned pretreating device processing is carried out Adsorption, and
The reverse osmosis membrane processing device, this reverse osmosis membrane processing device uses above-mentioned reverse osmosis membrane, and the second processing water of having been removed above-mentioned polyose composition by above-mentioned polyose absorbing treatment device is carried out desalination;
Described seawater desalination system also possesses:
The polyose concentration measuring mechanism, this polyose concentration measuring mechanism is measured the second polyose concentration of processing the first polyose concentration in the water and removed above-mentioned polyose composition above-mentioned the second processing water afterwards by above-mentioned polyose absorbing treatment device from above-mentioned first of above-mentioned pretreating device
Cleaning condition determination means, this cleaning condition determination means determine the cleaning condition of above-mentioned polyose sorbing material based on above-mentioned the first polyose concentration and the second polyose concentration measured by above-mentioned polyose concentration measuring mechanism, and
Wiper mechanism, this wiper mechanism cleans above-mentioned polyose sorbing material based on the cleaning condition that is determined by above-mentioned cleaning condition determination means.
2. seawater desalination system as claimed in claim 1 is characterized in that, sets a plurality of above-mentioned polyose absorbing treatment devices with respect to an above-mentioned reverse osmosis membrane processing device,
Described seawater desalination system constitutes, during by an above-mentioned polyose absorbing treatment device of above-mentioned wiper mechanism cleaning, carry out the Adsorption of above-mentioned polyose composition by the above-mentioned polyose absorbing treatment device of another one at least, can continue to carry out the above-mentioned second supply of processing water with respect to above-mentioned reverse osmosis membrane processing device.
3. seawater desalination system as claimed in claim 1 is characterized in that, any one in above-mentioned polyose absorbing treatment device use zeolite, gac, the clay intercalation compound is as above-mentioned polyose sorbing material.
4. seawater desalination system as claimed in claim 1, it is characterized in that above-mentioned cleaning condition determination means determines that in the temperature of the flow velocity of rinse water that the polyose sorbing material is cleaned, above-mentioned rinse water and the scavenging period at least one is as above-mentioned cleaning condition.
5. seawater desalination system as claimed in claim 1, it is characterized in that, above-mentioned cleaning condition determination means, based on the ratio of above-mentioned the second polyose concentration of having been removed above-mentioned polyose composition above-mentioned the second processing water afterwards by above-mentioned polyose absorbing treatment device with above-mentioned the first polyose concentration of having been removed above-mentioned polyose composition above-mentioned the first processing water before by above-mentioned polyose absorbing treatment device, determine above-mentioned cleaning condition.
CN201210265960.1A 2011-09-07 2012-07-26 Sea water desalination system Expired - Fee Related CN102976504B (en)

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