CN110510792A - Pretreatment unit and preprocess method for percolation liquid membrane concentrate MVR evaporation - Google Patents
Pretreatment unit and preprocess method for percolation liquid membrane concentrate MVR evaporation Download PDFInfo
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- CN110510792A CN110510792A CN201910738978.0A CN201910738978A CN110510792A CN 110510792 A CN110510792 A CN 110510792A CN 201910738978 A CN201910738978 A CN 201910738978A CN 110510792 A CN110510792 A CN 110510792A
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- 239000007788 liquid Substances 0.000 title claims abstract description 203
- 239000012528 membrane Substances 0.000 title claims abstract description 188
- 238000005325 percolation Methods 0.000 title claims abstract description 187
- 239000012141 concentrate Substances 0.000 title claims abstract description 183
- 238000000034 method Methods 0.000 title claims abstract description 40
- 238000001704 evaporation Methods 0.000 title claims abstract description 29
- 230000008020 evaporation Effects 0.000 title claims abstract description 28
- 238000006243 chemical reaction Methods 0.000 claims abstract description 171
- 239000000126 substance Substances 0.000 claims abstract description 59
- 238000005262 decarbonization Methods 0.000 claims abstract description 36
- 238000005189 flocculation Methods 0.000 claims abstract description 32
- 230000016615 flocculation Effects 0.000 claims abstract description 32
- 230000003750 conditioning effect Effects 0.000 claims abstract description 19
- 239000006228 supernatant Substances 0.000 claims abstract description 18
- 238000000926 separation method Methods 0.000 claims abstract description 16
- 238000005261 decarburization Methods 0.000 claims abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 194
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 75
- 229910052782 aluminium Inorganic materials 0.000 claims description 46
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 46
- 239000004411 aluminium Substances 0.000 claims description 38
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 34
- 229920002401 polyacrylamide Polymers 0.000 claims description 30
- 239000010802 sludge Substances 0.000 claims description 25
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 23
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 23
- 239000004571 lime Substances 0.000 claims description 23
- 230000000694 effects Effects 0.000 claims description 17
- 238000013019 agitation Methods 0.000 claims description 16
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims description 16
- -1 polypropylene Polymers 0.000 claims description 13
- 239000004743 Polypropylene Substances 0.000 claims description 12
- 239000002253 acid Substances 0.000 claims description 12
- 229920001155 polypropylene Polymers 0.000 claims description 12
- 239000002002 slurry Substances 0.000 claims description 10
- 150000001412 amines Chemical class 0.000 claims description 9
- 238000003756 stirring Methods 0.000 claims description 9
- 238000005352 clarification Methods 0.000 claims description 7
- 230000003311 flocculating effect Effects 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 7
- 238000010907 mechanical stirring Methods 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 abstract description 3
- 230000008016 vaporization Effects 0.000 abstract description 3
- 238000004062 sedimentation Methods 0.000 description 11
- 238000003801 milling Methods 0.000 description 8
- 239000010813 municipal solid waste Substances 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000012545 processing Methods 0.000 description 5
- HRPVXLWXLXDGHG-UHFFFAOYSA-N Acrylamide Chemical compound NC(=O)C=C HRPVXLWXLXDGHG-UHFFFAOYSA-N 0.000 description 4
- 239000003513 alkali Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 150000001408 amides Chemical class 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 238000011026 diafiltration Methods 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 230000006641 stabilisation Effects 0.000 description 2
- 238000011105 stabilization Methods 0.000 description 2
- 229920000742 Cotton Polymers 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010411 cooking Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000008595 infiltration Effects 0.000 description 1
- 238000001764 infiltration Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000001728 nano-filtration Methods 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000002829 reductive effect Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- 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
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The present invention relates to a kind of pretreatment units and preprocess method for percolation liquid membrane concentrate MVR evaporation, including conditioning tank, reaction cistern device, mechanical clarifier and decarbonization device, reaction cistern device is connected with flocculant chemicals dosing plant, the bottom of mechanical clarifier is connected to cistern device is reacted, and mechanical clarifier upper end is connected to decarbonization device, decarbonization device is communicated with MVR vaporising device；For its preprocess method the following steps are included: S1, flocculation, percolation liquid membrane concentrate enters in reaction cistern device by conditioning tank adds flocculant；S2, machinery are clarified, and the percolation liquid membrane concentrate after flocculation clarified separation, supernatant in mechanical clarifier flow to decarbonization device；S3, decarburization, the supernatant in mechanical clarifier flows to removing basicity is carried out in decarbonization device after enter MVR vaporising device.The present invention has the advantages that can reduce the hardness of percolation liquid membrane concentrate and basicity to meet MVR vaporization process conditions.
Description
Technical field
The present invention relates to the technical fields of percolation liquid membrane concentrate processing, more particularly, to a kind of percolation liquid membrane concentrate
The pretreatment unit and preprocess method of MVR evaporation.
Background technique
Percolate refer to rubbish during stacking and landfill due to physics, biology and the chemical action such as be compacted, ferment, simultaneously
A kind of waste water of the organic or inorganic ingredient of the high concentration generated under precipitation and the seepage effect of other external waters.China is raw
Rubbish living has moisture content height, and the high feature of rubbish from cooking content directly burns and easily causes the incinerator working of a furnace unstable, therefore
Fresh house refuse need to carry out fermentation in 5-7 days in garbage pool in garbage incinerating power plant, and to drip moisture removal, which is produced
Raw percolate accounts for 20% of garbage treatment quantity or so.
Percolate complicated component, heavy metal, organic pollutant concentration are high, and processing difficulty is big.In the practice process of many years,
China's garbage incinerating power plant has gradually formed the leachate treatment technology route of " biochemical treatment+film advanced treating ".It is nanofiltration, anti-
The membrane process such as infiltration can generate the film concentrate of a part while generating production water up to standard, it may be said that film concentrate is " concentration
Percolate ", it is more difficult because of enriched hardly degraded organic substance, inorganic salts and heavy metal, endanger bigger, percolate
If film concentrate cannot be effectively treated, environment will be caused great harm.
MVR is the abbreviation of mechanical steam recompression technology (mechanical vapor recompression), is utilized
Percolation liquid membrane concentrate can be evaporated by MVR technology, steam condensation, salt recycling disposal in solid form.Percolation liquid membrane concentration
Liquid hardness with higher and basicity, the fouling of heat-transfer surface is to influence one of the factor of MVR technical application in actual production, because
Before this MVR technique must by pre-process it is continuous, efficiently remove hardness and basicity in water body.
Summary of the invention
The first purpose of this invention is to provide a kind of hardness for reducing percolation liquid membrane concentrate and basicity to meet MVR
The pretreatment unit for percolation liquid membrane concentrate MVR evaporation of vaporization process conditions.
Second object of the present invention is to provide a kind of hardness for reducing percolation liquid membrane concentrate and basicity to meet MVR
The preprocess method for percolation liquid membrane concentrate MVR evaporation of vaporization process conditions.
To realize above-mentioned first purpose, the present invention provides the following technical scheme that a kind of be used for percolation liquid membrane concentrate
The pretreatment unit of MVR evaporation, including conditioning tank, the reaction water tank dress being sequentially communicated along percolation liquid membrane concentrate flow direction
It sets, for the mechanical clarifier of mud-water separation and for the decarbonization device to percolation liquid membrane concentrate removing basicity, the reaction
Cistern device is connected with flocculant chemicals dosing plant, and the bottom of the machinery clarifier is connected to the cistern device that reacts, and
The machinery clarifier upper end is connected to the decarbonization device, and the decarbonization device is communicated with MVR vaporising device.
By using above-mentioned technical proposal, when to the processing of percolation liquid membrane concentrate, percolation liquid membrane concentrate enters tune
It saves in pond, reaction water cabinet system is entered after homogeneous average, react and flocculant is added in cistern device, percolation liquid membrane concentrate wadding
It is solidifying, mud-water separation is carried out subsequently into mechanical clarifier, the supernatant in mechanical clarifier enters decarbonization device removing basicity, this
Invention reduces the hardness and basicity of percolation liquid membrane concentrate by technologies such as dosing flocculation, mechanical clarification and decarbonization devices, most
Hardness and the basicity control of the percolation liquid membrane concentrate entered in MVR vaporising device eventually are wanted in 1mmol/L hereinafter, meeting technique
It asks, and the water stabilization of percolation liquid membrane concentrate, strong operability in actual production process.
The present invention is further arranged to: the reaction cistern device include along percolation liquid membrane concentrate flow direction successively
The first reaction water tank, the second reaction water tank and the third of connection react water tank, and the flocculant chemicals dosing plant includes lime white
Chemical feed pipe, aluminium polychloride chemical feed pipe, sodium hydroxide chemical feed pipe, polyacrylamide chemical feed pipe, the lime white chemical feed pipe and institute
It states aluminium polychloride chemical feed pipe and reacts water tank connection with described first, the sodium hydroxide chemical feed pipe reacts water tank with described second
Connection, the polyacrylamide chemical feed pipe react water tank connection with the third.
By using above-mentioned technical proposal, pH is carried out to the percolation liquid membrane concentrate in the first reaction water tank by lime white
First successive step, flocculation is then carried out by aluminium polychloride and generates small floc sedimentation, then continues to adjust pH in the second water tank
Value, further occurrence effect of flocculant under the action of then in third reaction water tank in polyacrylamide, so that small floc sedimentation is formed
Big floc sedimentation improves percolation liquid membrane concentrate treatment effect to accelerate the sedimentation of solid content in water.
The present invention is further arranged to: being all provided in the first reaction water tank, the second reaction water tank and third reaction water tank
It is equipped with mechanical stirring device.
By using above-mentioned technical proposal, mechanical stirring device make react cistern device in percolation liquid membrane concentrate with
The medical fluid of addition can react more sufficiently completely.
The present invention is further arranged to: the mechanical clarifier bottom is connected with desliming device, and the desliming device includes
The sludge bucket being connected to the mechanical clarifier bottom is equipped with screw pump in the sludge bucket, and the screw pump is connected with plate
Frame deslimer.
By using above-mentioned technical proposal, the percolation liquid membrane concentrate after reaction cistern device flocculation enters mechanical clear
In clear device, flocculated alumen ustum filter in mechanical clarifier to be retained to mechanical clarifier bottom, into sludge bucket, then by from
Heart pump, which is delivered in decarbonizer, removes basicity.
The present invention is further arranged to: the decarbonization device includes the first decarbonizer and the second decarbonizer, and described first is de-
Acid solution chemicals dosing plant is provided between carbon device and the mechanical clarifier, between first decarbonizer and the second decarbonizer.
By using above-mentioned technical proposal, the removing twice that may be implemented for supernatant in mechanical clarifier is arranged such
Basicity, and add acid for adjusting pH value to meet the requirements before entering the first decarbonizer and the second decarbonizer, final dealkalize excellent effect.
The present invention is further arranged to: the decarbonization device further includes pipe-line mixer, the mechanical clarifier with it is described
Be provided with pipe-line mixer between first decarbonizer, first decarbonizer and the second decarbonizer, the pipe-line mixer with
The acid solution connection.
By using above-mentioned technical proposal, the setting of pipe-line mixer so that percolation liquid membrane concentrate and the concentrated sulfuric acid in pipeline
Enter after mixing in mixer and removes basicity in the first decarbonizer and the second decarbonizer.
The present invention is further arranged to: the acid solution chemicals dosing plant is concentrated sulfuric acid chemical feed pipe.
By using above-mentioned technical proposal, concentrated sulfuric acid acidity is stronger, can with higher efficiency complete dense for percolation liquid membrane
The adjusting of contracting liquid.
The present invention is further arranged to: the pipe-line mixer is internally provided with polytetrafluoroethylene ethylene layer.
By using above-mentioned technical proposal, so set, the concentrated sulfuric acid can be prevented for the corrosion inside pipe-line mixer,
Certain protective action is played to pipe-line mixer.
To realize above-mentioned second purpose, the present invention provides the following technical scheme that a kind of be used for percolation liquid membrane concentrate
The pretreating process of MVR evaporation uses a kind of above-mentioned pretreatment unit for percolation liquid membrane concentrate MVR evaporation to realize,
The following steps are included:
S1, flocculation, percolation liquid membrane concentrate enters in reaction cistern device by conditioning tank adds flocculant, in stirring condition
Under, percolation liquid membrane concentrate flows to mechanical clarifier after contacting with flocculant；
S2, machinery are clarified, and the clarified separation in mechanical clarifier of the percolation liquid membrane concentrate after flocculation, supernatant flows to decarburization dress
It sets；
S3, decarburization, the supernatant in mechanical clarifier flows to removing basicity is carried out in decarbonization device after enter MVR vaporising device.
By using above-mentioned technical proposal, by adding flocculant into reaction cistern device, so that percolation liquid membrane is concentrated
Enter after liquid flocculation and carry out mud-water separation in mechanical clarifier, the supernatant in mechanical clarifier enters decarbonization device removing alkali
Degree reduces the basicity and hardness of percolation liquid membrane concentrate with clarified separation by flocculating, then is further decreased by decarbonization device
The basicity and hardness of percolation liquid membrane concentrate, finally by the hardness of percolation liquid membrane concentrate and basicity control in 1mmol/L hereinafter,
Meet technique requirement, and treated percolation liquid membrane concentrate water stabilization, strong operability in actual production process.
The present invention is further arranged to: the reaction cistern device used in step S1 includes that liquid stream is concentrated along percolation liquid membrane
The first reaction water tank, the second reaction water tank and the third reaction water tank that dynamic direction is sequentially communicated, the first reaction water tank connect
It is connected with lime white chemical feed pipe and aluminium polychloride chemical feed pipe, the second reaction water tank is communicated with sodium hydroxide chemical feed pipe, described
Third reaction water tank is communicated with polyacrylamide chemical feed pipe；
Flocculant in step S1 includes aluminium polychloride and polyacrylamide, concrete operations are as follows: percolation liquid membrane concentrate passes through
Conditioning tank enters in the first reaction water tank, and the feeding lime slurry into the first reaction water tank adjusts percolate in the first reaction water tank
The pH of film concentrate is 8, and aluminium polychloride is added, and keeping the polyaluminium aluminum concentration in the first reaction water tank is 15-25g/L,
Under agitation, contact residence time of the percolation liquid membrane concentrate with aluminium polychloride is 1- in the first reaction of control water tank
2h reacts in water tank so that percolation liquid membrane concentrate flows to second after initial flocculation effect occurs with aluminium polychloride；
It is flowed in third reaction water tank after adding sodium hydroxide into the second reaction water tank, so that flowing in third reaction water tank
The pH value of percolation liquid membrane concentrate is 11-13.5, and polypropylene milling amine is then added into third reaction water tank, keeps third reaction
Concentration of polyacrylamide in water tank is 10-15mg/L, and controls percolation liquid membrane concentrate and polypropylene in third reaction water tank
The contact residence time of amide is 1-2h, and then percolation liquid membrane concentrate flows to mechanical clarifier.
The present invention is further arranged to: mechanical clarifier bottom is communicated with sludge bucket in step S2, is equipped in sludge bucket
Screw pump, screw pump are connected with sheet frame deslimer；
The concrete operations of step S2 are as follows: the percolation liquid membrane concentrate after flocculating in step S1, which enters, carries out muddy water in mechanical clarifier
Separation, sludge is delivered to sheet frame deslimer after entering sludge bucket under the action of helicoidal pump, the supernatant in mechanical clarifier into
Enter in decarbonization device.
By using above-mentioned technical proposal, mechanical clarifier realizes the muddy water point of the percolation liquid membrane concentrate after flocculation
From.
The present invention is further arranged to: the decarbonization device in step S3 includes the first decarbonizer and the second decarbonizer, described
Between first decarbonizer and the mechanical clarifier, pipeline is provided between first decarbonizer and the second decarbonizer mixes
Device, the pipe-line mixer are connected with concentrated sulfuric acid chemical feed pipe；
The concrete operations of step S3 are as follows: supernatant flows to the pipeline between the first decarbonizer and mechanical clarifier in mechanical clarifier
In mixer, the concentrated sulfuric acid is added into the pipe-line mixer, so that mixed percolation liquid membrane concentrate and concentrated sulfuric acid mixture
PH value less than 4.7 after enter the first decarbonizer remove basicity；
Then enter in the pipe-line mixer between the first decarbonizer and the second decarbonizer from the outflow of the first decarbonizer, to the pipeline
Mixer adds the concentrated sulfuric acid so that the pH value of mixed percolation liquid membrane concentrate and concentrated sulfuric acid mixture less than 4.7 after enter
Second decarbonizer removes basicity, and the percolation liquid membrane concentrate after removing basicity enters MVR vaporising device from the outflow of the second decarbonizer.
By using above-mentioned technical proposal, is realized by the first decarbonizer and the second decarbonizer and contracting liquid is done for percolation liquid membrane
Removing basicity twice, finally the hardness of percolation liquid membrane concentrate and basicity control are wanted hereinafter, meeting technique in 1mmol/L
It asks.
In conclusion advantageous effects of the invention are as follows:
1, in the present invention by reaction cistern device, mechanical clarification and the setting of decarbonization device from dosing flocculation, mechanical clarification with
And the technologies such as removing basicity reduce the hardness and basicity of percolation liquid membrane concentrate, eventually enter into the percolate in MVR vaporising device
The hardness and basicity of film concentrate are controlled in 1mmol/L hereinafter, meeting technique requirement, and the water quality of percolation liquid membrane concentrate is steady
It is fixed, strong operability in actual production process；
2, percolation liquid membrane concentrate is flocculated first by flocculation, mechanical clarification and the setting of decarbonization process in the present invention
Hardness and basicity in percolation liquid membrane concentrate are greatly lowered after separation, it is then de- by the first decarbonizer and the second decarbonizer again
Except basicity so that eventually enter into the percolation liquid membrane concentrate in MVR vaporising device hardness and basicity control 1mmol/L with
Under；
3, pass through the first reaction water tank, the second reaction water tank, third reaction water tank and flocculant chemicals dosing plant in the present invention
Setting, which is realized, flocculates to percolation liquid membrane concentrate using aluminium polychloride, and percolation liquid membrane is concentrated using polyacrylamide
The floc sedimentation that liquid helps solidifying formation bigger, improves flocculating effect；
4, the present invention in pipe-line mixer setting so that percolation liquid membrane concentrate and the concentrated sulfuric acid be sufficiently mixed after enter first take off
Basicity is removed in carbon device and the second decarbonizer, so that dealkalize excellent effect.
Detailed description of the invention
Fig. 1 is overall structure diagram of the invention.
In figure, 1, conditioning tank；2, cistern device is reacted；21, the first reaction water tank；22, the second reaction water tank；23, third
React water tank；3, mechanical clarifier；31, sludge bucket；32, sheet frame deslimer；4, decarbonization device；41, the first decarbonizer；42,
Two decarbonizers；43, pipe-line mixer；5, flocculant chemicals dosing plant；51, lime white chemical feed pipe；52, aluminium polychloride chemical feed pipe；
53, sodium hydroxide chemical feed pipe；54, polyacrylamide chemical feed pipe；6, concentrated sulfuric acid chemical feed pipe.
Specific embodiment
Below in conjunction with attached drawing, invention is further described in detail.
It referring to Fig.1, is a kind of pretreatment unit for percolation liquid membrane concentrate MVR evaporation disclosed by the invention, including
Conditioning tank 1, reaction cistern device 2 and the mechanical clarifier 3 being sequentially communicated along percolation liquid membrane concentrate flow direction, reaction water
Case apparatus 2 is connected to the bottom of mechanical clarifier 3, and 3 upper end of mechanical clarifier is communicated with decarbonization device 4,4 pairs of decarbonization device diafiltrations
Liquid film concentration removing basicity, the bottom end of mechanical clarifier 3 are communicated with desliming device, and desliming device includes and mechanical clarifier 3
The sludge bucket 31 of bottom connection, sludge bucket 31 are connected with screw pump, and screw pump is connected with sheet frame deslimer 32.React cistern device
2 are connected with flocculant chemicals dosing plant 5, and decarbonization device 4 is communicated with MVR vaporising device.
When to the processing of percolation liquid membrane concentrate, percolation liquid membrane concentrate enters in conditioning tank 1, enters after homogeneous average
Cistern device 2 is reacted, addition flocculant in cistern device 2 is reacted and flocculates to form alumen ustum, percolation liquid membrane concentrate and alumen ustum mixing
Liquid enters mechanical clarifier 3 and is separated, and mechanical clarifier 3 is the prior art, is mainly situated between using one or several kinds of filterings
Matter removes the impurity such as the alumen ustum of percolation liquid membrane concentrate by medium, passes through reaction in application scheme under pressure
Mixture after cistern device 2 flocculates enters from the bottom of mechanical clarifier 3, and the medium in mechanical clarifier 3 is in mixture
Alumen ustum carry out retention filtering and form sludge, sludge enters in the sludge bucket 31 under mechanical clarifier 3, by screw pump by sludge
It is delivered to sheet frame deslimer 32 and carries out Treatment of Sludge, and the supernatant in mechanical clarifier 3 enters in decarbonization device 4 and removes alkali
Degree.The present invention is flocculated by dosing, machinery is clarified and the hardness and alkali of the technologies such as decarbonization device 4 reduction percolation liquid membrane concentrate
Degree, the hardness and basicity for eventually entering into the percolation liquid membrane concentrate in MVR vaporising device are controlled in 1mmol/L hereinafter, meeting work
Skill requirement.
Reaction cistern device 2 include be sequentially communicated along percolation liquid membrane concentrate flow direction first reaction water tank 21,
Second reaction water tank 22 and third react water tank 23, and the first reaction water tank 21, second reacts water tank 22 and third reacts water tank
Mechanical stirring device is provided in 23.The flocculated flocculant of percolation liquid membrane concentrate can not be limited in the present invention, only needed
Reach flocculating effect, preferably selection aluminium polychloride and polyacrylamide, aluminium polychloride is to adjust diafiltration to be processed
The charge of liquid film concentrate is to allow the solid content in percolation liquid membrane concentrate to generate small floc sedimentation, but this floc sedimentation is too small,
The rate of settling is inadequate, therefore polyacrylamide is added, and small floc sedimentation is further wadded a quilt with cotton combinate form at big by bind-mechanism by polyacrylamide
Floc sedimentation is to accelerate the sedimentation of solid content in water.By inventor's many experiments, find aluminium polychloride in the case where pH is 8
Flocculating effect it is more preferable, polyacrylamide pH be 12.5 in the case where effect of flocculant it is more preferable.
Therefore flocculant chemicals dosing plant 5 includes lime white chemical feed pipe 51, aluminium polychloride chemical feed pipe 52, sodium hydroxide chemical feed pipe
53, polyacrylamide chemical feed pipe 54, lime white chemical feed pipe 51 and aluminium polychloride chemical feed pipe 52 react water tank 21 with first and are connected to,
Sodium hydroxide chemical feed pipe 53 reacts water tank 22 with second and is connected to, and polyacrylamide chemical feed pipe 54 reacts the connection of water tank 23 with third.
It is 8 to pH to the first successive step of the percolation liquid membrane concentrate progress pH in the first reaction water tank 21 by lime white, then passes through
Aluminium polychloride is once flocculated, and then continues the pH value of adjustment percolation liquid membrane concentrate extremely in the second reaction water tank 22
12.5, it is reacted into third and accelerates sedimentation in water tank 23 under the action of polyacrylamide, improve the processing of percolation liquid membrane concentrate
Effect, the setting of mechanical stirring device is so that the first reaction water tank 21, second reacts in water tank 22 and third reaction water tank 23
Percolation liquid membrane concentrate and the medical fluid of addition can react more sufficiently completely, improve flocculating effect.And first reaction water
The substance that pH value is adjusted in case 21 selects lime white, and lime white is the common raw material of semidry method depickling in garbage incinerating power plant,
Operating cost is advantageously reduced to successive step at the beginning of pH using lime white in the present invention.
Decarbonization device 4 include the first decarbonizer 41 being connected to at the top of mechanical clarifier 3 and with 41 bottom of the first decarbonizer
Second decarbonizer 42 of connection, decarbonizer are existing equipment, can be directly commercially available, and principle is mainly fixed according to Henry
Rule, i.e., the gas flow being dissolved in quantitative liquid under certain temperature is proportional to the partial pressure that balance is in solution, in air blast
Under the action of machine, the intracorporal carbon dioxide of water is blown out, to achieve the purpose that remove basicity.Generally use decarbonizer removing alkali
When spending, decarbonizer inlet flow-patterm is needed 4.7 hereinafter, former decarbonization device 4 further includes acid solution chemicals dosing plant, to entrance decarburization dress
The adjusting that the percolation liquid membrane concentrate in 4 carries out pH is set, acid solution herein does not limit, it is only necessary to which realization will enter the first decarbonizer
41 and the second percolation liquid membrane concentrate in decarbonizer 42 to adjust pH be 4.7 or less.Preferred acid solution is dense sulphur in the present invention
Acid, acid solution chemicals dosing plant selects concentrated sulfuric acid chemical feed pipe 6, acid stronger, and it is higher to adjust pH value efficiency.
In order to enable the mixing of percolation liquid membrane concentrate and the concentrated sulfuric acid is more uniform, mechanical clarifier 3 and the first decarbonizer
41, be provided with pipe-line mixer 43 between the first decarbonizer 41 and the second decarbonizer 42, and two pipe-line mixers 43 with it is dense
Sulfuric acid chemical feed pipe 6 mixes.So set, when the supernatant flowed out out of mechanical clarifier 3 passes through pipe-line mixer 43, with
The concentrated sulfuric acid of addition is sufficiently mixed, and the pH for adjusting percolation liquid membrane concentrate enters removing in the first decarbonizer 41 after being 4.7 or less
Basicity is mixed subsequently into the pipe-line mixer 43 between the first decarbonizer 41 and the second decarbonizer 42 with the concentrated sulfuric acid of addition
Uniformly, the pH for adjusting percolation liquid membrane concentrate enters in the second decarbonizer 42 after being 4.7 or less removes basicity, subsequently into MVR
Percolation liquid membrane concentrate is carried out secondary dealkalize operation by vaporising device, eventually enters into the percolation liquid membrane concentration in MVR vaporising device
The hardness and basicity of liquid are controlled in 1mmol/L hereinafter, meeting technique requirement.
Carry out the adjusting of basicity and hardness in compared to the prior art to percolation liquid membrane concentrate using decarbonizer completely, this
In invention using the technologies such as dosing flocculation, mechanical clarification and decarbonizer removing basicity reduce percolation liquid membrane concentrate hardness and
Basicity reduces the amount for using the concentrated sulfuric acid, and realizes the hardness of filtrate film concentrate and basicity control is laggard in 1mmol/L or less
Enter MVR vaporising device, meets technique requirement.
Because need to be added the concentrated sulfuric acid in pipe-line mixer 43, therefore pipe-line mixer 43 is internally provided with polytetrafluoroethyl-ne
Alkene layer.The concentrated sulfuric acid can be prevented for the corrosion inside pipe-line mixer 43, certain protection is played to pipe-line mixer 43 and is made
With.
Connection in the present invention between all parts feature can be to be connected to by pipeline, it is only necessary to realize that percolation liquid membrane is dense
Contracting liquid can flow to next reaction part from last part, be adapted to the actuators such as the addition centrifugal pump of shape to facilitate and seep
Filtrate film concentrate can flow to next reaction part from last part, this is those skilled in the art's conventional means, the present invention
In be no longer described in detail.
The present invention also provides realize pretreatment using the above-mentioned pretreatment unit for percolation liquid membrane concentrate MVR evaporation
Method, comprising the following steps:
S1, flocculation, percolation liquid membrane concentrate enter in the first reaction water tank 21 by conditioning tank 1, into the first reaction water tank 21
Feeding lime slurry, the pH for adjusting percolation liquid membrane concentrate in the first reaction water tank 21 is 7.5-8.5, and aluminium polychloride, In is added
Under stirring condition, keeping the polyaluminium aluminum concentration in the first reaction water tank 21 is 15-25g/L, under agitation, control the
Contact residence time of the percolation liquid membrane concentrate with aluminium polychloride is 1-2h in one reaction water tank 21, so that percolation liquid membrane is concentrated
Liquid flows to second after initial flocculation effect occurs with aluminium polychloride and reacts in water tank 22；
It adds and is flowed to after sodium hydroxide in third reaction water tank 23 into the second reaction water tank 22, under agitation, control the
Percolation liquid membrane concentrate and sodium hydroxide contact residence time are 1.5h in two reaction water tanks 22, and flow to third reaction water tank 23
The pH value of interior percolation liquid membrane concentrate is 11-13.5, and polypropylene milling amine is then added into third reaction water tank 23, keeps the
Concentration of polyacrylamide in three reaction water tanks 23 is 10-15mg/L, and controls percolation liquid membrane concentration in third reaction water tank 23
Contact residence time of the liquid with polyacrylamide is 1-2h；
S2, clarified separation, percolation liquid membrane concentrate, which enters, carries out mud-water separation in mechanical clarifier 3, sludge enters sludge bucket 31
Sheet frame deslimer 32 is delivered under the action of helicoidal pump afterwards, the supernatant in mechanical clarifier 3 enter the first decarbonizer 41 with
In pipe-line mixer 43 between mechanical clarifier 3；
S3, decarburization add the concentrated sulfuric acid into the pipe-line mixer 43 between the first decarbonizer 41 and mechanical clarifier 3, must be added
The pH value of percolation liquid membrane concentrate after the concentrated sulfuric acid less than 4.7 after enter the first decarbonizer 41 and remove basicity, then percolation liquid membrane
Concentrate enters in the pipe-line mixer 43 between the first decarbonizer 41 and the second decarbonizer 42 from the outflow of the first decarbonizer 41, to
The pipe-line mixer 43 adds the concentrated sulfuric acid, so that the pH value of mixed percolation liquid membrane concentrate and concentrated sulfuric acid mixture is less than
After 4.7 enter the second decarbonizer 42 remove basicity, remove basicity after percolation liquid membrane concentrate from the second decarbonizer 42 flow out into
Enter MVR vaporising device.
The aluminium polychloride and polyacrylamide used in the present invention is common flocculant in the art.
Embodiment 1
A kind of preprocess method for percolation liquid membrane concentrate MVR evaporation uses above-mentioned for percolation liquid membrane concentrate MVR
The pretreatment unit of evaporation is realized, comprising the following steps:
S1, flocculation, percolation liquid membrane concentrate enter in the first reaction water tank 21 by conditioning tank 1, into the first reaction water tank 21
Feeding lime slurry, the pH for adjusting percolation liquid membrane concentrate in the first reaction water tank 21 is 8, aluminium polychloride is added, in stirring bar
Under part, keeping the polyaluminium aluminum concentration in the first reaction water tank 21 is 20g/L, under agitation, controls the first reaction water
In case 21 contact residence time of the percolation liquid membrane concentrate with aluminium polychloride be 1.5h so that percolation liquid membrane concentrate with polymerize
Aluminium chloride flows in the second reaction water tank 22 after initial flocculation effect occurs；
It adds and is flowed to after sodium hydroxide in third reaction water tank 23 into the second reaction water tank 22, under agitation, control the
Percolation liquid membrane concentrate and sodium hydroxide contact residence time are 1.5h in two reaction water tanks 22, and flow to third reaction water tank 23
The pH value of interior percolation liquid membrane concentrate is 12.5, and polypropylene milling amine is then added into third reaction water tank 23, keeps third
Concentration of polyacrylamide in reaction water tank 23 is 12mg/L, and controls percolation liquid membrane concentrate in third reaction water tank 23 and gather
The contact residence time of acrylamide is 1.5h；
S2, clarified separation, percolation liquid membrane concentrate, which enters, carries out mud-water separation in mechanical clarifier 3, sludge enters sludge bucket 31
Sheet frame deslimer 32 is delivered under the action of helicoidal pump afterwards, the supernatant in mechanical clarifier 3 enter the first decarbonizer 41 with
In pipe-line mixer 43 between mechanical clarifier 3；
S3, decarburization add the concentrated sulfuric acid into the pipe-line mixer 43 between the first decarbonizer 41 and mechanical clarifier 3, must be added
The pH value of percolation liquid membrane concentrate after the concentrated sulfuric acid less than 4.7 after enter the first decarbonizer 41 and remove basicity, then percolation liquid membrane
Concentrate enters in the pipe-line mixer 43 between the first decarbonizer 41 and the second decarbonizer 42 from the outflow of the first decarbonizer 41, to
The pipe-line mixer 43 adds the concentrated sulfuric acid, so that the pH value of mixed percolation liquid membrane concentrate and concentrated sulfuric acid mixture is less than
After 4.7 enter the second decarbonizer 42 remove basicity, remove basicity after percolation liquid membrane concentrate from the second decarbonizer 42 flow out into
Enter MVR vaporising device.
Embodiment 2
A kind of preprocess method for percolation liquid membrane concentrate MVR evaporation, carries out, difference according to method in embodiment 1
It is:
S1, flocculation, percolation liquid membrane concentrate enter in the first reaction water tank 21 by conditioning tank 1, into the first reaction water tank 21
Feeding lime slurry, the pH for adjusting percolation liquid membrane concentrate in the first reaction water tank 21 is 7.5, and aluminium polychloride is added, is stirring
Under the conditions of, keeping the polyaluminium aluminum concentration in the first reaction water tank 21 is 15g/L, under agitation, the first reaction of control
In water tank 21 contact residence time of the percolation liquid membrane concentrate with aluminium polychloride be 1h so that percolation liquid membrane concentrate with polymerize
Aluminium chloride flows in the second reaction water tank 22 after initial flocculation effect occurs；
It adds and is flowed to after sodium hydroxide in third reaction water tank 23 into the second reaction water tank 22, under agitation, control the
Percolation liquid membrane concentrate and sodium hydroxide contact residence time are 1h in two reaction water tanks 22, and are flowed in third reaction water tank 23
Percolation liquid membrane concentrate pH value be 11, then to third reaction water tank 23 in add polypropylene milling amine, keep third reaction
Concentration of polyacrylamide in water tank 23 is 10mg/L, and controls percolation liquid membrane concentrate and polypropylene in third reaction water tank 23
The contact residence time of amide is 1h.
Embodiment 3
A kind of preprocess method for percolation liquid membrane concentrate MVR evaporation, carries out, difference according to method in embodiment 1
It is:
S1, flocculation, percolation liquid membrane concentrate enter in the first reaction water tank 21 by conditioning tank 1, into the first reaction water tank 21
Feeding lime slurry, the pH for adjusting percolation liquid membrane concentrate in the first reaction water tank 21 is 8.5, and aluminium polychloride is added, is stirring
Under the conditions of, keeping the polyaluminium aluminum concentration in the first reaction water tank 21 is 25g/L, under agitation, the first reaction of control
In water tank 21 contact residence time of the percolation liquid membrane concentrate with aluminium polychloride be 2h so that percolation liquid membrane concentrate with polymerize
Aluminium chloride flows in the second reaction water tank 22 after initial flocculation effect occurs；
It adds and is flowed to after sodium hydroxide in third reaction water tank 23 into the second reaction water tank 22, under agitation, control the
Percolation liquid membrane concentrate and sodium hydroxide contact residence time are 2h in two reaction water tanks 22, and are flowed in third reaction water tank 23
Percolation liquid membrane concentrate pH value be 13.5, then to third reaction water tank 23 in add polypropylene milling amine, keep third it is anti-
Answering the concentration of polyacrylamide in water tank 23 is 15mg/L, and controls percolation liquid membrane concentrate and poly- third in third reaction water tank 23
The contact residence time of acrylamide is 2h.
Embodiment 4
A kind of preprocess method for percolation liquid membrane concentrate MVR evaporation, carries out, difference according to method in embodiment 1
It is:
S1, flocculation, percolation liquid membrane concentrate enter in the first reaction water tank 21 by conditioning tank 1, into the first reaction water tank 21
Feeding lime slurry, the pH for adjusting percolation liquid membrane concentrate in the first reaction water tank 21 is 8, aluminium polychloride is added, in stirring bar
Under part, keeping the polyaluminium aluminum concentration in the first reaction water tank 21 is 20g/L, under agitation, controls the first reaction water
In case 21 contact residence time of the percolation liquid membrane concentrate with aluminium polychloride be 1.5h so that percolation liquid membrane concentrate with polymerize
Aluminium chloride flows in the second reaction water tank 22 after initial flocculation effect occurs；
It adds and is flowed to after sodium hydroxide in third reaction water tank 23 into the second reaction water tank 22, under agitation, control the
Percolation liquid membrane concentrate and sodium hydroxide contact residence time are 1.5h in two reaction water tanks 22, and flow to third reaction water tank 23
The pH value of interior percolation liquid membrane concentrate is 11, and polypropylene milling amine is then added into third reaction water tank 23, keeps third anti-
Answering the concentration of polyacrylamide in water tank 23 is 12mg/L, and controls percolation liquid membrane concentrate and poly- third in third reaction water tank 23
The contact residence time of acrylamide is 1.5h.
Embodiment 5
A kind of preprocess method for percolation liquid membrane concentrate MVR evaporation, carries out, difference according to method in embodiment 1
It is:
S1, flocculation, percolation liquid membrane concentrate enter in the first reaction water tank 21 by conditioning tank 1, into the first reaction water tank 21
Feeding lime slurry, the pH for adjusting percolation liquid membrane concentrate in the first reaction water tank 21 is 8, aluminium polychloride is added, in stirring bar
Under part, keeping the polyaluminium aluminum concentration in the first reaction water tank 21 is 20g/L, under agitation, controls the first reaction water
In case 21 contact residence time of the percolation liquid membrane concentrate with aluminium polychloride be 1.5h so that percolation liquid membrane concentrate with polymerize
Aluminium chloride flows in the second reaction water tank 22 after initial flocculation effect occurs；
It adds and is flowed to after sodium hydroxide in third reaction water tank 23 into the second reaction water tank 22, under agitation, control the
Percolation liquid membrane concentrate and sodium hydroxide contact residence time are 1.5h in two reaction water tanks 22, and flow to third reaction water tank 23
The pH value of interior percolation liquid membrane concentrate is 13.5, and polypropylene milling amine is then added into third reaction water tank 23, keeps third
Concentration of polyacrylamide in reaction water tank 23 is 12mg/L, and controls percolation liquid membrane concentrate in third reaction water tank 23 and gather
The contact residence time of acrylamide is 1.5h.
Comparative example 1
A kind of preprocess method for percolation liquid membrane concentrate MVR evaporation, carries out, difference according to method in embodiment 1
It is:
S1, flocculation, percolation liquid membrane concentrate enter in the first reaction water tank 21 by conditioning tank 1, into the first reaction water tank 21
Feeding lime slurry, the pH for adjusting percolation liquid membrane concentrate in the first reaction water tank 21 is 8, aluminium polychloride is added, in stirring bar
Under part, keeping the polyaluminium aluminum concentration in the first reaction water tank 21 is 20g/L, under agitation, controls the first reaction water
In case 21 contact residence time of the percolation liquid membrane concentrate with aluminium polychloride be 1.5h so that percolation liquid membrane concentrate with polymerize
Aluminium chloride flows in the second reaction water tank 22 after initial flocculation effect occurs；
It adds and is flowed to after sodium hydroxide in third reaction water tank 23 into the second reaction water tank 22, under agitation, control the
Percolation liquid membrane concentrate and sodium hydroxide contact residence time are 1.5h in two reaction water tanks 22, and flow to third reaction water tank 23
The pH value of interior percolation liquid membrane concentrate is 8, and polypropylene milling amine is then added into third reaction water tank 23, keeps third reaction
Concentration of polyacrylamide in water tank 23 is 12mg/L, and controls percolation liquid membrane concentrate and polypropylene in third reaction water tank 23
The contact residence time of amide is 1.5h.
Above-described embodiment 1-5 and comparative example 1 are used for the pretreatment of the percolation liquid membrane concentrate of identical water quality by performance detection,
It is discharged after the water outlet of conditioning tank 1, the water outlet of 3 supernatant of mechanical clarifier and 42 decarburization of the second decarbonizer and carries out respectively in step sl
The measurement of the hardness and basicity of water quality, measurement result are as shown in table 1 below.
Table 1:
It is by upper table 1 it is found that by flocculation, mechanical clarification and the setting of decarbonization process that percolation liquid membrane concentrate is first in the present invention
Hardness and basicity in percolation liquid membrane concentrate is greatly lowered after first carrying out flocculation separation, then passes through the first decarbonizer and the again
Two decarbonizers remove basicity so that eventually enter into the percolation liquid membrane concentrate in MVR vaporising device hardness and basicity control exist
1mmol/L is hereinafter, meet technique requirement.
The embodiment of present embodiment is presently preferred embodiments of the present invention, not limits protection of the invention according to this
Range, therefore: the equivalence changes that all structures under this invention, shape, principle are done, should all be covered by protection scope of the present invention it
It is interior.
Claims (10)
1. a kind of pretreatment unit for percolation liquid membrane concentrate MVR evaporation, it is characterised in that: including dense along percolation liquid membrane
Conditioning tank (1) that contracting liquid flow direction is sequentially communicated, reaction cistern device (2), for mud-water separation mechanical clarifier (3) and
For the decarbonization device (4) to percolation liquid membrane concentrate removing basicity, the reaction cistern device (2) is connected with flocculant dosing
Cistern device (2) connection, and the mechanical clarifier (3) are reacted with described in device (5), the bottom of the mechanical clarifier (3)
Upper end is connected to the decarbonization device (4), and the decarbonization device (4) is communicated with MVR vaporising device.
2. a kind of pretreatment unit for percolation liquid membrane concentrate MVR evaporation according to claim 1, feature exist
In: reaction cistern device (2) includes the first reaction water tank being sequentially communicated along percolation liquid membrane concentrate flow direction
(21), the second reaction water tank (22) and third reaction water tank (23), the flocculant chemicals dosing plant (5) includes lime white dosing
Manage (51), aluminium polychloride chemical feed pipe (52), sodium hydroxide chemical feed pipe (53), polyacrylamide chemical feed pipe (54), the lime
Slurry chemical feed pipe (51) and the aluminium polychloride chemical feed pipe (52) react water tank (21) with described first and are connected to, the sodium hydroxide
Chemical feed pipe (53) reacts water tank (22) connection, the polyacrylamide chemical feed pipe (54) and the third reaction water with described second
Case (23) connection.
3. a kind of pretreatment unit for percolation liquid membrane concentrate MVR evaporation according to claim 2, feature exist
In: mechanical stirring is provided in first reaction water tank (21), the second reaction water tank (22) and third reaction water tank (23)
Device.
4. a kind of pretreatment unit for percolation liquid membrane concentrate MVR evaporation according to claim 1, feature exist
In: mechanical clarifier (3) bottom is connected with desliming device, and the desliming device includes and the mechanical clarifier (3) bottom
The sludge bucket (31) of portion's connection, the sludge bucket (31) is interior to be equipped with screw pump, and the screw pump is connected with sheet frame deslimer
(32)。
5. a kind of pretreatment unit for percolation liquid membrane concentrate MVR evaporation according to claim 1, feature exist
In: the decarbonization device (4) include the first decarbonizer (41) and the second decarbonizer (42), first decarbonizer (41) with it is described
Acid solution chemicals dosing plant is provided between mechanical clarifier, between first decarbonizer (41) and the second decarbonizer (42).
6. a kind of pretreatment unit for percolation liquid membrane concentrate MVR evaporation according to claim 5, feature exist
In: the decarbonization device (4) further includes pipe-line mixer (43), the mechanical clarifier (3) and first decarbonizer (41),
Pipe-line mixer (43), the pipe-line mixer are provided between first decarbonizer (41) and the second decarbonizer (42)
(43) it is connected to the chemicals dosing plant, the acid solution chemicals dosing plant is concentrated sulfuric acid chemical feed pipe (6).
7. a kind of preprocess method for percolation liquid membrane concentrate MVR evaporation, it is characterised in that: it uses claim 1 institute
A kind of pretreatment unit for percolation liquid membrane concentrate MVR evaporation stated is realized, comprising the following steps:
S1, flocculation, percolation liquid membrane concentrate enters in reaction cistern device (2) by conditioning tank (1) adds flocculant, is stirring
Under the conditions of, percolation liquid membrane concentrate flows to mechanical clarifier (3) after contacting with flocculant；
S2, mechanical clarification, for the percolation liquid membrane concentrate after flocculation in mechanical clarifier (3) interior clarified separation, supernatant flow direction is de-
Carbon device (4)；
S3, decarburization, the supernatant in mechanical clarifier (3) flows to removing basicity is carried out in decarbonization device (4) after enter MVR and evaporate
Device.
8. a kind of preprocess method for percolation liquid membrane concentrate MVR evaporation according to claim 7, feature exist
In: the reaction cistern device (2) used in step S1 includes be sequentially communicated along percolation liquid membrane concentrate flow direction first
Water tank (21), the second reaction water tank (22) and third reaction water tank (23) are reacted, first reaction water tank (21) is communicated with
Lime white chemical feed pipe (51) and aluminium polychloride chemical feed pipe (52), second reaction water tank (22) are communicated with sodium hydroxide dosing
It manages (53), third reaction water tank (23) is communicated with polyacrylamide chemical feed pipe (54)；
Flocculant in step S1 includes aluminium polychloride and polyacrylamide, concrete operations are as follows: percolation liquid membrane concentrate passes through
Conditioning tank (1) enters in the first reaction water tank (21), to the interior feeding lime slurry of the first reaction water tank (21), adjusts the first reaction water
The pH of the interior percolation liquid membrane concentrate of case (21) is 7.5-8.5, and aluminium polychloride is added, and keeps poly- in the first reaction water tank (21)
Conjunction concentration of aluminum chloride is 15-25g/L, and under agitation, control first is reacted water tank (21) interior percolation liquid membrane concentrate and gathered
The contact residence time for closing aluminium chloride is 1-2h, so that after initial flocculation effect occurs for percolation liquid membrane concentrate and aluminium polychloride
It flows in the second reaction water tank (22)；
It is flowed in third reaction water tank (23) after adding sodium hydroxide into the second reaction water tank (22), so that flowing to third reaction
The pH value of percolation liquid membrane concentrate in water tank (23) is 11-13.5, then adds polypropylene into third reaction water tank (23)
Amine is milled, keeping the concentration of polyacrylamide in third reaction water tank (23) is 10-15mg/L, and controls third reaction water tank (23)
Contact residence time of the interior percolation liquid membrane concentrate with polyacrylamide is 1-2h, and then percolation liquid membrane concentrate flow direction is mechanical clear
Clear device (3).
9. a kind of preprocess method for percolation liquid membrane concentrate MVR evaporation according to claim 8, feature exist
In: mechanical clarifier (3) bottom is communicated with sludge bucket (31) in step S2, is equipped with screw pump, screw pump in sludge bucket (31)
It is connected with sheet frame deslimer (32)；
The concrete operations of step S2 are as follows: the percolation liquid membrane concentrate after flocculating in step S1, which enters in mechanical clarifier (3), to carry out
Mud-water separation, sludge are delivered to sheet frame deslimer (32), mechanical clarifier after entering sludge bucket (31) under the action of helicoidal pump
(3) supernatant in enters in decarbonization device (4).
10. a kind of preprocess method for percolation liquid membrane concentrate MVR evaporation according to claim 8, feature exist
In: the decarbonization device (4) in step S3 includes the first decarbonizer (41) and the second decarbonizer (42), first decarbonizer (41)
It is mixed that pipeline is provided between the mechanical clarifier (3), between first decarbonizer (41) and the second decarbonizer (42)
Clutch (43), the pipe-line mixer (43) are connected with concentrated sulfuric acid chemical feed pipe (6)；
The concrete operations of step S3 are as follows: mechanical clarifier (3) interior supernatant flows to the first decarbonizer (41) and mechanical clarifier (3)
Between pipe-line mixer (43) in, to the concentrated sulfuric acid is added in the pipe-line mixer (43), so that mixed percolation liquid membrane is dense
The pH value of contracting liquid and concentrated sulfuric acid mixture less than 4.7 after enter the first decarbonizer (41) remove basicity；
Then it is mixed from the pipeline that the first decarbonizer (41) outflow enters between the first decarbonizer (41) and the second decarbonizer (42)
In device (43), the concentrated sulfuric acid is added to the pipe-line mixer (43), so that mixed percolation liquid membrane concentrate and concentrated sulfuric acid mixing
The pH value of object less than 4.7 after enter the second decarbonizer (42) and remove basicity, the percolation liquid membrane concentrate after removing basicity is from second
Decarbonizer (42) outflow enters MVR vaporising device.
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