CN104386769B - Method for selectively extracting salt from high-salinity organic wastewater - Google Patents
Method for selectively extracting salt from high-salinity organic wastewater Download PDFInfo
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- CN104386769B CN104386769B CN201410620106.1A CN201410620106A CN104386769B CN 104386769 B CN104386769 B CN 104386769B CN 201410620106 A CN201410620106 A CN 201410620106A CN 104386769 B CN104386769 B CN 104386769B
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- 150000003839 salts Chemical class 0.000 title claims abstract description 212
- 239000002351 wastewater Substances 0.000 title claims abstract description 147
- 238000000034 method Methods 0.000 title claims abstract description 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 113
- 238000005406 washing Methods 0.000 claims abstract description 40
- 210000003141 lower extremity Anatomy 0.000 claims description 70
- 238000002425 crystallisation Methods 0.000 claims description 67
- 230000008025 crystallization Effects 0.000 claims description 67
- 239000010413 mother solution Substances 0.000 claims description 20
- 239000012452 mother liquor Substances 0.000 claims description 18
- 238000007701 flash-distillation Methods 0.000 claims description 11
- 239000010815 organic waste Substances 0.000 claims description 11
- 239000012530 fluid Substances 0.000 claims description 10
- 238000000605 extraction Methods 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 9
- 238000005507 spraying Methods 0.000 claims 1
- 239000002245 particle Substances 0.000 abstract description 11
- 238000004065 wastewater treatment Methods 0.000 abstract description 6
- 238000004140 cleaning Methods 0.000 abstract description 5
- 238000007599 discharging Methods 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 abstract description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 22
- 239000013078 crystal Substances 0.000 description 18
- 239000003344 environmental pollutant Substances 0.000 description 13
- 238000001704 evaporation Methods 0.000 description 13
- 231100000719 pollutant Toxicity 0.000 description 13
- 230000008020 evaporation Effects 0.000 description 12
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 10
- 239000007787 solid Substances 0.000 description 10
- 239000000243 solution Substances 0.000 description 9
- 239000012267 brine Substances 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 239000007921 spray Substances 0.000 description 8
- 239000000126 substance Substances 0.000 description 8
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 6
- 159000000000 sodium salts Chemical class 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000011780 sodium chloride Substances 0.000 description 5
- 238000010025 steaming Methods 0.000 description 5
- 239000000047 product Substances 0.000 description 4
- 239000002910 solid waste Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 230000000903 blocking effect Effects 0.000 description 3
- 238000005119 centrifugation Methods 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 239000010842 industrial wastewater Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 210000003205 muscle Anatomy 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 238000001223 reverse osmosis Methods 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 239000006200 vaporizer Substances 0.000 description 2
- NWZSZGALRFJKBT-KNIFDHDWSA-N (2s)-2,6-diaminohexanoic acid;(2s)-2-hydroxybutanedioic acid Chemical compound OC(=O)[C@@H](O)CC(O)=O.NCCCC[C@H](N)C(O)=O NWZSZGALRFJKBT-KNIFDHDWSA-N 0.000 description 1
- 241001529739 Prunella <angiosperm> Species 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- PFLUPZGCTVGDLV-UHFFFAOYSA-N acetone azine Chemical compound CC(C)=NN=C(C)C PFLUPZGCTVGDLV-UHFFFAOYSA-N 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004581 coalescence Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- IKDUDTNKRLTJSI-UHFFFAOYSA-N hydrazine monohydrate Substances O.NN IKDUDTNKRLTJSI-UHFFFAOYSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 239000008258 liquid foam Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000011833 salt mixture Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- SRWFBFUYENBCGF-UHFFFAOYSA-M sodium;chloride;hydrochloride Chemical compound [Na+].Cl.[Cl-] SRWFBFUYENBCGF-UHFFFAOYSA-M 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000032258 transport Effects 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/14—Purification
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/16—Purification
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention provides a method for selectively extracting salt from high-salinity organic wastewater. The method for selectively extracting the salt from the high-salinity organic wastewater comprises the following steps: firstly, heating to-be-treated wastewater to be in an overheated state; secondly, causing the overheated wastewater obtained in the step one to enter a flash tank from a circulating water inlet to be subjected to flashing, causing wastewater obtained after the flashing is carried out to enter a circulating pipeline from a circulating water outlet and repeating the step one, and causing crystallized salt particles to enter a salt washing leg; thirdly, injecting the to-be-treated wastewater from a water inlet in the upper part of the salt washing leg downward, and cleaning the crystallized salt particles; fourthly, injecting the to-be-treated wastewater from a water inlet in the middle part of the salt washing leg, so that at least one part of the cleaned crystallized salt particles does centrifugal movement and is discharged from a salt discharging hole of the salt washing leg; and fifthly, separating the crystallized salt particles and wastewater which are discharged out from the salt discharging hole. The method for selectively extracting the salt from the high-salinity organic wastewater has the advantages that the crystallized salt particles can be washed for multiple times under the condition that the crystallized salt particles and wastewater are mixed, wastewater treatment efficiency is high, cost is low, and purity of the obtained crystallized salt particles is high.
Description
Technical field
The present invention relates to a kind of processing method of salt-containing organic wastewater；More particularly, it relates to it is a kind of
The method of selective extraction salinity from high salt organic waste water.
Background technology
In various large scale industries produce, such as oil refining, Coal Chemical Industry, electric power, fine chemistry industry, printing and dyeing and
Pharmacy etc., can produce substantial amounts of salt-containing organic wastewater.Because China is the water resource country that there is a serious shortage in the supply, lead to
Often these waste water can be required reuse, but these waste water, after by reuse, can produce a small amount of high salt organic waste
Water, mainly contains the pollutant such as various inorganic salinities and Organic substance in waste water.Contain due in these high-salt wastewaters
There are above-mentioned pollutant, typically can not directly discharge, and need to continue to concentrate by waste water, realize the zero-emission of waste water
Put or near-zero release.At present, the common technology flow process realizing wastewater zero discharge is as follows:
Industrial wastewater → pretreatment and biochemistry → ultrafiltration → reverse osmosiss (ro) → ro concentrated water membrance concentration system → steaming
Send out → crystallization.
In process above, after processing through reverse-osmosis treated and membrance concentration system, total salinity (tds) in waste water
Mass fraction bring up to 5%-8%, wastewater flow rate greatly reduces.Very small amount of waste water then enters in vaporizer
Step evaporation, makes Waste water concentrating reach more than 21% to the wherein mass fraction of tds.Finally, steam through vaporizer
Haline water after sending out is delivered to and is carried out re-evaporation in crystallizer, forms crystal salt, realizes the zero-emission of waste water.
For example, Chinese patent 201310205628.0 discloses the technique that a kind of strong brine evaporates liquid zero emission
Method, the method comprises the steps: that (1) is delivered directly to evaporation through the strong brine of pretreatment by pump
Device is processed；(2) by air preheater, 50-100 DEG C is heated to normal temperature air using heat source medium,
Obtain hot-air；(3) step (2) gained hot-air is transported in vaporising device, sets inside vaporising device
The deflector put carries out heat exchange, by air quantity control with the strong brine being delivered in vaporising device through step (1)
System, makes the gas and water temperature control within vaporising device below 60 DEG C；The flowing of hot-air makes on deflector
Produce negative pressure around the hole opened and accelerate moisture evaporation, discharge saturation hot-air；Inside vaporising device,
Strong brine is circulated with 70 times of circulating load by circulating pump on deflector, and constantly concentrates；When dense salt
When water is concentrated into setting tds value, the high concentration brine sludge of the critical crystal state below 60 obtaining DEG C passes through salt
Dredge pump is discharged, and enters equipment for separating liquid from solid and carries out saline separation, respectively obtains solid state crystallization salt and supernatant；
(4), after step (3) is processed, the solid state crystallization salt obtaining fills or further Treatment for Reuse, obtains
Supernatant is back to vaporising device and continues with.
Although through pretreatment and biochemical treatment for high salt organic waste water, but wherein still contain
A certain amount of Organic substance, using being crystal salt including more Organic substance obtained by process above method, can only
Carry out special filling up or further Treatment for Reuse.Taking a certain medium-and-large-sized coal chemical industry enterprises as a example, one produces 20 per year
The enterprise of billion cubic meter natural gas from coal, the solid waste producing per hour more than 3 tons, by danger per ton
Solid waste landfill needs 3000 yuan of calculating, and annual landfill expense is 72,000,000 yuan and (runs 8000 by annual
Hour meter).This can not bear so huge landfill expense for enterprise.
Component analyses are carried out by the solid waste that wastewater zero discharge is produced it has been found that wherein inorganic
Salt accounts for absolute majority, particularly nacl and na2so4Component, the content of general both salt is more than 90%.Cause
This, if by nacl and na2so4Separated with other materials, then the solid that can reduce more than 90% gives up
Gurry, substantially reduces the expense of solid waste landfill, obtains nacl, na simultaneously2so4Salt-mixture is as sal prunella
The raw material of coproduction industry, turns waste into wealth, and produces certain economic benefit.This point to be realized, needs to meet
Claimed below: nacl, the na 1, separating2so4Must be very pure, reach the relevant of country and industry
Standard；2nd, control the concentration of other pollutant it is impossible to nacl, na2so4Crystallize simultaneously, and must simultaneously
The output very little of wastewater mother liquor must be ensured, that is, the concentration of other pollutant is dense enough.
Chinese patent 201210525944.1 discloses a kind of ketazine process and produces the wastewater treatment of hydrazine hydrate and carry
The method of salt, it sequentially comprises the following steps: the 1) recovery of brine waste and storage；2) waste water preheating rises
Temperature；3) waste water evaporative crystallization, vapor is condensed to become entrance cold water storage tank after condensed water, and condensed water changes
Enter biochemical treatment station after heat drop temperature, reclaim and storage as brine waste after crystalline mother solution and oxidant reaction；
4) salt slurry centrifugation, centrifuge mother liquor returns evaporative crystallization and recycles；5) wet salt send saturated brine to wash,
Obtain pure salt slurry；6) pure salt slurry centrifugation, centrifuge mother liquor delivers to saturated brine cycles of washing profit again
With.
Chinese patent 201010590105.9 discloses a kind of processing method of glycerinated high salt industrial wastewater,
Comprising: the industrial wastewater containing glycerol and high-load sodium chloride is removed moisture through evaporation process, receive respectively
Collection evaporation water and solid sodium chloride, this solid sodium chloride hydrochloric acid solution washs to remove glycerol, is then peeled off
Glycerinated hydrochloric acid solution, obtains the solid sodium chloride of purification.
Technique scheme is by the purity improving crystal salt to the crystal salt method washed, its shortcoming
It is to need first with waste water, the crystal salt obtained by evaporation to be carried out solid-liquid separation, crystal salt could be entered afterwards
Row washing, leads to the inefficiency of wastewater treatment and salt extraction.
Content of the invention
For the deficiencies in the prior art, it is an object of the invention to provide one kind selectivity from high salt organic waste water
The method extracting salinity, the method can be carried out to crystallization salt grain in the state of crystallization salt grain is mixed with waste water
Washing.
For achieving the above object, the invention provides a kind of selective extraction salinity from high salt organic waste water
Method, comprising:
1. heat pending waste water so as to be in superheat state；
2. make that step is 1. obtained to be crossed thermal wastewater and carry out flash distillation by circulating water inlet and enter in flash tank；Flash distillation
1. obtained waste water enter circulating line repeat step by circulating water outlet, and crystallize salt grain and then enter salt
Washing lower limb；
3. pending waste water is sprayed into downwards by the top water inlet that salt washs lower limb, crystallization salt grain is carried out；
4. pending waste water is sprayed into by salt washing midleg water inlet, the knot after making at least a portion be cleaned by
Brilliant salt grain is made centrifugal motion and is discharged by the salt outlet that salt washs lower limb；
5. the crystallization salt grain discharged by salt outlet and waste water are separated.
In the present invention, high salt organic waste water refer to that sodium salt content is its dissolved solution degree more than 50%, other
Pollutant load is the salt-containing organic wastewater of less than the 5% of its dissolved solution degree.From raising efficiency, reduce energy
From the point of view of consumption, it is the 60% of its dissolved solution degree that the method for the present invention is preferred for processing sodium salt content
Above high salt organic waste water, being more preferably used for processing sodium salt content is more than the 75% of its dissolved solution degree
High salt organic waste water.
In the present invention, it is possible to use forced circulation heat exchanger heats to waste water, it is overheated useless that heating obtains
Water is delivered in flash tank through circulating line and carries out flash distillation, due to the evaporation of moisture, in the thermal wastewater after concentration
Nacl and na2so4Reach hypersaturated state, separate out nacl, na2so4Crystal grain.Due to its density be greater than useless
The density of water, crystal grain moves downwardly in salt washing lower limb with the flowing of thermal wastewater and action of gravity, in fortune
Constantly mutually collide during dynamic, combine and " growing up ".
The crystallization salt grain being entered by flash tank and thermal wastewater are with the pending waste water being sprayed into by top water inlet in salt
It is sufficiently mixed in washing lower limb.Preferably, top water inlet is located at salt and washs on the longitudinal axis of lower limb, forms circle
Tapered current spray into, and it is useless with sprayed into by top water inlet to make the crystallization salt grain being entered by flash tank and thermal wastewater
Water has more sufficient mixed effect.Due to nacl, na in pending waste water2so4Content higher, or even
Close to its saturated concentration, and the concentration of other pollutant reaches far away saturation, therefore nacl, na2so4Can be basic
Keep the crystal grain being formed, and reach saturation and be attached to other pollutant of grain surface and can again dissolve,
That is, the waste water being sprayed into by top water inlet can be to nacl, the na preliminarily forming2so4Crystal grain plays washing
Effect, thus obtain pure nacl, na2so4Crystal grain.Therefore, the method for the present invention can be in crystallization salt grain
In the state of mixing with waste water, crystallization salt grain is washed, waste water treatment efficiency is high.
In the present invention, using pending waste water, crystallization salt grain is carried out, cost for wastewater treatment is low.This
Outward, the waste water for cleaning crystallization salt grain can enter in circulating line to make salt extraction after separating with crystallization salt grain
Process, the final wastewater flow rate therefore obtained by the present invention is considerably less.Contrary, in the prior art,
It is introduced into what other cleanout fluid beyond pending waste water were carried out to crystallization salt grain, this does not only result in waste water
The increase of processing cost, and final wastewater flow rate is more, because these cleanout fluid containing pollutant also can become
For a kind of new waste water.
In the present invention, middle part water inlet can be vortex filament shape curved surface entrance, tangent line shape entrance, spiral yarn shaped enter
Mouth, concentric circular annular entry, involute shape entrance, arc line shaped entrance or spiral of Archimedes shape entrance,
Crystallization salt grain is driven to make centrifugal motion so that producing eddy flow by the waste water that middle part water inlet sprays into.Due to centrifugation
Effect, the larger crystallization salt grain of particle diameter moves to the inwall that salt washs lower limb, and circles arrival salt outlet,
Thus discharging salt washing lower limb, and move in the bottom that thinner crystallization salt grain then continues to wash lower limb to salt.Meanwhile,
The waste water being sprayed into by middle part water inlet also can play further cleaning function to crystallization salt grain.
In the present invention, it is possible to use the waterwater entrance being arranged on circulating line supplements waste water into circulating line.
Preferably, the wastewater flow in unit interval internal recycle pipeline is at least 100 times of the wastewater flow replenishing,
More preferably at least 150 times, thus less to the components influence of waste water in circulating line.
According to a specific embodiment of the present invention, the method for the present invention is also included using the bottom being washed lower limb by salt
The pending waste water that portion's water inlet sprays into makes the crystallization salt grain moving to salt washing lower limb bottom move upwards.Preferably
Ground, bottom water inlet is located at salt and washs on the longitudinal axis of lower limb, sprays into downwards waste water.
As described above, moving in the bottom that the relatively fine crystallization salt grain do not discharged from salt outlet washs lower limb to salt, and by
The waste water that bottom water inlet sprays into makes crystallization salt grain move upwards, during moving upwards, transports with downward
The crystallization salt grain of larger particle is collided, combined to form to dynamic crystallization salt grain, thus can discharge from salt outlet, because
This, can obtain granularity and more uniformly crystallize salt grain.Particularly when bottom water inlet sprays into waste water downwards,
Waste water promote first thinner crystallization salt grain move downwardly to salt washing lower limb bottom after again back towards upper motion, show
The probability write lifting crystallization salt grain collision, combining, makes crystallization salt grain quickly grow up and discharges from salt outlet.
Meanwhile, the waste water being sprayed into by bottom water inlet equally has cleaning action to crystallization salt grain, further reduces
The content of Organic substance in crystallization salt grain.
According to another embodiment of the present invention, the method for the present invention also includes first waste water being carried out dense
The step of contracting.The waste water of the salinity to be extracted of the major part after concentration is delivered to circulating line, and fraction is to be extracted
The waste water of salinity then enters in salt washing lower limb.For example, in the case of the sodium salt content of waste water is not sufficiently high,
Although sodium salt can be extracted from waste water using said method, there is energy consumption and processing cost is higher not
Foot.At this point it is possible to waste water be concentrated further using saline water evaporators such as falling film evaporations.For example, by waste water
Be concentrated into that sodium salt content is its dissolved solution degree 80% about, that is, be closer to the dissolubility under its room temperature,
And other pollutant are due to it, and concentration of itself in waste water is not high, so, its concentration is relatively still very
Low, far below the dissolubility under its room temperature.
According to another embodiment of the present invention, the step of the inventive method 2. in, at least a portion mistake
Thermal wastewater enters the bottom of flash tank by second circulation water inlet and/or salt washs the top of lower limb, and remaining is overheated
Waste water is then entered in flash tank by positioned at the first circulation water inlet on second circulation water inlet.
Preferably, 5-15% volume cross thermal wastewater by second circulation water inlet enter flash tank bottom and/or
Salt washs the top of lower limb, and the thermal wastewater of crossing of 85-95% volume is entered in flash tank by first circulation water inlet.
In the present invention, second circulation water inlet can be arranged on flash tank and salt washs the intersection of lower limb, also may be used
Wash the top of lower limb with the bottom or salt being arranged on flash tank.
In the present invention, cross thermal wastewater in be partly into flash tank bottom and/or washing lower limb top and
Discharge, the vapour transmission thermal wastewater of formation discharges to the top of flash tank herein, steam during rising,
Form bubble, to nacl, the na being formed in its top thermal wastewater as " brush "2so4Crystal grain is cleaned,
Make to be attached to nacl, na2so4Other pollutant such as Organic substance of grain surface are redissolved in thermal wastewater.Wipe
Nacl, na after washing2so4Crystal grain then enters in salt washing lower limb, and is washed by the waste water that top water inlet is sprayed into
Wash.Certainly, it is preferably controlled in appropriate scope by the waste water that second circulation water inlet enters, with preferably
Play the effect cleaning crystal grain.
Therefore, in the method for the present invention, crystallization salt grain is repeatedly cleaned during it is grown up,
Therefore, even if other pollutant in crystal salt intragranular portion are also effectively removed.On the contrary, in prior art
In, crystallization salt grain is just washed after being separated with waste water, and therefore prior art can only clean crystallization
Other pollutant on salt grain surface, and then helpless to being wrapped in its other internal pollutant.
According to another embodiment of the present invention, set between first circulation water inlet and circulating water outlet
Put stop the two directly relative to recirculation baffle plate.Recirculation baffle plate guiding crystallization salt grain is moved to salt washing lower limb,
Reduce the crystal salt grain number amount moved to circulating water outlet, with prevent crystal salt grain blocking circulating water outlet and/or
Circulating line, it is to avoid produce short circuit phenomenon during waste water circulation.
Preferably, recirculation baffle plate covers circulating water outlet from the top of circulating water outlet and has court obliquely
Salt washs the inclined surface of lower limb top droop, makes waste water enter circulating water outlet under recirculation baffle plate, keeps away
Exempt from crystallization salt grain to be directly deposited at circulating water outlet with waste water.
According to another embodiment of the present invention, after extracting salinity, obtained wastewater mother liquor is by being arranged on
Mother solution discharge-channel on circulating line is discharged, and mother solution discharge-channel has mother solution entrance and mother liquor outlet, female
Liquid entrance is located at the lower section of mother liquor outlet.
When waste water in flash tank enters circulating line, more or less can entrainment portions crystallization salt grain enter into
In circulating line.In the present invention, mother solution entrance is arranged on the lower section of mother liquor outlet, due to crystallizing the ratio of salt grain
The great proportion in wastewater mother liquor, when waste discharge mother solution, under gravity, crystallization salt grain is transported downwards
Dynamic, and wastewater mother liquor then can be discharged from the mother liquor outlet of high point, by simple Gravity Separation, can will crystallize
Salt grain is separated with wastewater mother liquor, effectively prevents from crystallizing salt grain with mother solution discharge.
According to another embodiment of the present invention, the top that salt washs in lower limb is provided with washs lower limb along salt
The drain part of longitudinal extension, crystallization salt grain is limited along the periphery wall of drain part and the internal perisporium of salt washing lower limb
Annular fluid passage move downward.Preferably, drain part is extended to enter with top by the top that salt washs lower limb
The substantially concordant position in the mouth of a river.The cross-sectional area of annular fluid passage washs what lower limb lumenal cross-section amassed for salt
1/8-7/8, preferably 1/4-1/2.
In the present invention, the cross-sectional area of annular fluid passage is less than the cross-sectional area that salt washs lower limb inner chamber, therefore,
Compared with the situation being not provided with drain part, crystallization salt grain can be from flash tank quickly under salt washing lower limb
Portion moves.Additionally, the inwall that crystallization salt grain washs lower limb near salt in annular fluid passage moves downward, can
Quickly to be discharged, improve the treatment effeciency of waste water by salt outlet.
According to another embodiment of the present invention, waste water washs the tangential direction of lower limb inwall by middle part along salt
Water inlet enters in salt washing lower limb, just be can reach by simple tangent line shape entry design and so that salt is washed in lower limb
Crystallization salt grain and solution mixture form the purpose of eddy flow.
According to another embodiment of the present invention, the water that enters circulating water inlet is directed downward, and is located at sudden strain of a muscle
On the longitudinal axis of steaming pot, made thermal wastewater along the radially uniform distribution of flash tank, made full use of flash tank
Flash distillation area, makes flash process uniformly and stably carry out and violent boiling phenomenon does not occur, and reduces abrasion.
Preferably, circulation water inlet enters at it and has, on water direction, the cross-sectional area being gradually increased, and makes circulation pipe
Thermal wastewater of crossing in road enters in flash tank after slowing down, it is to avoid liquid foam entrainment and short circuit.
Compared with prior art, the method for the present invention can be to knot in the state of crystallization salt grain is mixed with waste water
Brilliant salt grain is repeatedly washed, and waste water treatment efficiency is high, low cost, and obtained crystallization salt grain purity is high.
Below in conjunction with drawings and Examples, the present invention is described in further detail.
Brief description
Fig. 1 is the structural representation of the evaporation and crystallization system embodiment realizing the inventive method；
Fig. 2 is the structural representation of flash tank in Fig. 1；
Fig. 3 is the structural representation that in Fig. 1, salt washs lower limb；
Fig. 4 is the structural representation of mother solution separator in Fig. 1.
Specific embodiment
As shown in figure 1, the evaporation and crystallization system embodiment realizing the inventive method includes: circulating line 10,
(in figure is not shown for circulating pump 20, heater 30, flash tank 40, salt washing lower limb 50 and equipment for separating liquid from solid
Go out).
Circulating line 10 is vertically arranged, and has substantially u shape structure, and two vertical arm are close with flash tank 40 respectively
Envelope connect, be arranged on the circulating pump 20 at circulating line 10 bottom fold realize waste water circulating line 10,
Circulating in heater 30 and flash tank 40.Waste water inlet 11 and mother are provided with the first vertical arm
Liquid/gas separator 12, and waste water inlet 11 is located at the lower section of mother solution separator 12.Waste water inlet 11 is used for following
The waste water of salinity to be extracted is inputted, mother solution separator 12 is used for discharging gained after extraction salinity in endless tube road 10
The wastewater mother liquor arriving.
Heater 30 is arranged in the second vertical arm of circulating line 10, for will enter flash tank 40
Waste water heated to reach superheat state.Heater 30 is forced circulation heat exchanger, steam by
Steam inlet 31 positioned at forced circulation heat exchanger top inputs, and the condensed fluid being formed after heat exchange is from being arranged on
The leakage fluid dram 32 of forced circulation heat exchanger bottom is discharged.
As shown in Fig. 2 flash tank 40 is vertically arranged, include small end coniform steaming upward from top to bottom successively
Vapour is discharged section 41, columned flash distillation segment occurred 42 and small end coniform product directed downwardly and is discharged section 43.
In conjunction with shown in Fig. 1-3, split into two strands after the waste water in circulating line 10 is heated, wherein most
Cross thermal wastewater entered by the first circulation water positioned at flash distillation segment occurred 42 bottom through circulating line the first branch line 13
Mouth 421 is downwardly into flash distillation segment occurred 42, and the thermal wastewater excessively of remaining fraction is through circulating line the second branch line 14
Sudden strain of a muscle is downwardly into by the second circulation water inlet 431 washing lower limb 50 intersection positioned at product discharge section 43 and salt
The bottom of steaming pot 40 and the top of salt washing lower limb 50.First circulation water inlet 421 and second circulation water inlet
431 are big end cone shaped opening directed downwardly, and are arranged on the longitudinal axis of flash tank 40.First circulation
Water inlet 421 is limited by conical distribution baffle plate 4211 to be obtained.The steam that flash distillation produces is by being arranged on steaming
The steam outlet 411 that vapour discharges section 41 top is discharged, and the most of waste water in flash tank 40 is by being arranged on
The circulating water outlet 432 that product discharges section 43 side wall enters to make to repeat to process in circulating line 10, and remains
Then syncrystallization salt grain enters in salt washing lower limb 50 remaining small part waste water.
Above circulating water outlet 432, set between first circulation water inlet 421 and circulating water outlet 432
It is equipped with recirculation baffle plate 433, the side that recirculation baffle plate 433 discharges section 43 from product extends and has oblique
The inclined surface of the lower top droop washing lower limb 50 towards salt, to cover from above circulating water outlet 432 and to guide
Move in the direction that crystallization salt grain washs lower limb 50 to salt, it is to avoid crystallization salt grain blocking circulating water outlet 432, and makes
Crystallization salt grain as few as possible is entered in circulating line 10 by circulating water outlet 432.
In conjunction with shown in Fig. 1 and Fig. 3, salt washing lower limb 50 is directly connected to flash tank 40, and the longitudinal direction of the two
Axis is overlapping.The top that salt washs in lower limb 50 is provided with drain part 51, and it is fixed on brine wash by support rod
Wash on the inwall of lower limb 50.Drain part 51 is the hollow pipe of upper end closed, and its diameter is about in salt washing lower limb 50
The 1/2 of chamber diameter, crystallization salt grain and waste water limit along the periphery wall of drain part 51 and the internal perisporium of salt washing lower limb 50
The annular fluid passage 511 made moves downward.In drain part 51, the position near drain part 51 bottom sets
It is equipped with top water inlet 52, top water inlet 52 is located at salt and washs on the longitudinal axis of lower limb 50, salt to be extracted
The waste water dividing is formed down pyramid type current by top water inlet 52 and sprays into.The lower section of top water inlet 52 sets
Be equipped with the middle part water inlet 53 that the tangential direction washing lower limb 50 inwall along salt extends, the waste water of salinity to be extracted by
Middle part water inlet 53 enters in salt washing lower limb 50, makes crystallization salt grain and solution mixture form eddy flow, from
Under heart effect, the larger crystallization salt grain of particle diameter moves to the inwall that salt washs lower limb 50, and circles, and arrives
Reach the salt outlet 54 positioned at middle part water inlet 53 lower section, washed the tangent line of lower limb 50 inwall by salt outlet 54 along salt
Direction is discharged, and thinner crystallization salt grain then continues to move downward.The lower section of salt outlet 54 is provided with bottom
Water inlet 55, bottom water inlet 55 is located at salt and washs on the longitudinal axis of lower limb 50 and wash lower limb 50 near salt
Bottom.Bottom water inlet 55 sprays into downwards the waste water of salinity to be extracted, so that thinner crystallization salt grain is moved upwards,
The crystallization salt grain moved upwards and the crystallization salt grain moving downward constantly mutually are collided, are tied coalescence, thus
Can be discharged by salt outlet 54, prevent crystallization salt grain from blocking in bottom deposit and be arranged on salt washing lower limb 50 bottom
Sewage draining exit 56.
Salt outlet 54 is connected with equipment for separating liquid from solid, and equipment for separating liquid from solid separates the knot discharged by salt outlet 54
Brilliant salt grain and waste water, thus obtain pure crystallization salt grain.
Top water inlet 52, middle part water inlet 53 and bottom water inlet 55 are respectively connecting to the first waste water supply
Pipeline 60, waste water inlet 11 connects to the second waste water service (not shown), the first waste water supply
Pipeline 60 and the second waste water service connect to waste water source, such as through the waste water obtained by evaporation and concentration in advance
(not shown).First flushing water inlet 61, circulating line are provided with the first waste water service 60
Second flushing water inlet 141 is provided with the second branch line 14.
As shown in figure 4, mother solution separator 12 limits two mother solution discharge-channels 121, each mother solution discharge
Passage 121 is respectively provided with mother solution entrance 1211 and mother liquor outlet 1212, each mother solution entrance 1211 position respectively
Lower section in corresponding mother liquor outlet 1212.At predetermined time intervals, that is, when waste water makes wherein through circular treatment
When the content of Organic substance reaches certain numerical value, make wastewater mother liquor pass through mother solution discharge-channel 121 and discharge.
Using above-mentioned evaporation and crystallization system embodiment selective extraction salinity from high salt organic waste water method such as
Under:
1. heat pending waste water so as to be in superheat state；
2. at least a portion making step 1. obtained is crossed thermal wastewater and is entered flash tank by second circulation water inlet
Bottom and/or salt wash the top of lower limb, and remaining crosses thermal wastewater then by the on second circulation water inlet
One circulation water inlet enters in flash tank, and the waste water obtained by flash distillation enters circulating line simultaneously by circulating water outlet
1. repeat step, and crystallizes salt grain and then enters salt washing lower limb；
3. pending waste water is sprayed into downwards by the top water inlet that salt washs lower limb, crystallization salt grain is carried out；
4. pending waste water is sprayed into by salt washing midleg water inlet, make to be cleaned by the larger crystallization of rear particle diameter
Salt grain is made centrifugal motion and is discharged by the salt outlet that salt washs lower limb；
5. the crystallization salt grain discharged by salt outlet and waste water are separated；
6. obtained wastewater mother liquor after discharge extraction salinity.
Although the present invention is disclosed above with preferred embodiment, it is not limited to the scope of present invention enforcement.
Those of ordinary skill in the art, in the invention scope without departing from the present invention, according to the present invention made same
Deng improvement, the invention scope that should be the present invention is covered.
Claims (10)
1. a kind of method of selective extraction salinity from high salt organic waste water, comprising:
1. heat pending waste water so as to be in superheat state；
2. make that step is 1. obtained to be crossed thermal wastewater and carry out flash distillation by circulating water inlet and enter in flash tank；Flash distillation
1. obtained waste water enter circulating line repeat step by circulating water outlet, and crystallize salt grain and then enter salt
Washing lower limb；
3. pending waste water is sprayed into downwards by the top water inlet that described salt washs lower limb, crystallization salt grain is carried out clearly
Wash；
4. pending waste water is sprayed into by described salt washing midleg water inlet, after so that at least a portion is cleaned by
Crystallization salt grain make centrifugal motion and by described salt wash lower limb salt outlet discharge；
5. the crystallization salt grain discharged by described salt outlet and waste water are separated.
2. the method for claim 1, it is also included using the bottom water inlet being washed lower limb by described salt
The pending waste water spraying into makes the crystallization salt grain moving to described salt washing lower limb bottom move upwards.
3. the method for claim 1, it also includes the step first waste water being concentrated.
4. the method for claim 1, wherein step 2. in, at least a portion cross thermal wastewater by
Second circulation water inlet enters the bottom of described flash tank and/or described salt washs the top of lower limb, and remaining is overheated
Waste water is then entered in described flash tank by positioned at the first circulation water inlet on described second circulation water inlet.
5. method as claimed in claim 4, wherein, the thermal wastewater of crossing of 5-15% volume is followed by described second
Ring water inlet enters the bottom of described flash tank and/or described salt washs the top of lower limb, 85-95% volume overheated
Waste water is entered in described flash tank by described first circulation water inlet.
6. method as claimed in claim 4, wherein, in described first circulation water inlet and described recirculated water
Between outlet setting stop the two directly relative to recirculation baffle plate.
7. after the method for claim 1, wherein extracting salinity, obtained wastewater mother liquor is by arranging
Mother solution discharge-channel on described circulating line is discharged, and described mother solution discharge-channel has mother solution entrance and mother
Liquid exports, and described mother solution entrance is located at the lower section of described mother liquor outlet.
8. the top that the method for claim 1, wherein described salt washs in lower limb is provided with along described
Salt washs the drain part of the longitudinal extension of lower limb, and crystallization salt grain is washed along the periphery wall of described drain part and described salt
The annular fluid passage that the internal perisporium of lower limb is limited moves downward.
9. the method for claim 1, wherein waste water washs the tangential direction of lower limb inwall along described salt
Entered in described salt washing lower limb by described middle part water inlet.
10. the method for claim 1, wherein the water that enters of described circulation water inlet is directed downward,
And on the longitudinal axis of described flash tank.
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| CN201603419U (en) * | 2009-12-10 | 2010-10-13 | 自贡市轻工业设计研究院有限责任公司 | Salt elutriation device |
| CN102557164B (en) * | 2010-12-15 | 2013-12-11 | 益海嘉里(连云港)化工有限公司 | Recycling method of high-salt industrial wastewater containing glycerin |
| CN202638034U (en) * | 2012-05-15 | 2013-01-02 | 中国中轻国际工程有限公司 | Lysine hydrochloride evaporation crystallization tank |
| CN103011503B (en) * | 2012-12-06 | 2014-01-15 | 广州新普利节能环保科技有限公司 | Method and device for wastewater treatment and salt extraction during hydrazine hydrate production by ketazine process |
| CN103342398B (en) * | 2013-07-17 | 2015-03-25 | 山东潍坊润丰化工股份有限公司 | Method for recovering high-purity organic salt from phosphorous-containing industrial wastewater |
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Effective date of registration: 20170119 Address after: Guangzhou Tianhe District City, Guangdong province forest road and poly central block A 1507 Patentee after: GUANGZHOU HANTAI ENVIRONMENTAL TECHNOLOGY CO., LTD. Address before: 422309 Shaoyang, Hunan Province garden town, Garden Town, garden village, No. 30 Patentee before: Zeng Xiaofang Patentee before: Jing Lina |