CN109534584A - A kind of organic silicon wastewater processing system and method - Google Patents
A kind of organic silicon wastewater processing system and method Download PDFInfo
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- 239000002351 wastewater Substances 0.000 title claims abstract description 130
- 238000012545 processing Methods 0.000 title claims abstract description 47
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 title claims abstract description 44
- 229910052710 silicon Inorganic materials 0.000 title claims abstract description 44
- 239000010703 silicon Substances 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title abstract description 17
- 230000000694 effects Effects 0.000 claims abstract description 261
- 238000001704 evaporation Methods 0.000 claims abstract description 131
- 230000008020 evaporation Effects 0.000 claims abstract description 130
- 238000010612 desalination reaction Methods 0.000 claims abstract description 28
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 12
- 239000007787 solid Substances 0.000 claims abstract description 11
- 238000002425 crystallisation Methods 0.000 claims abstract description 7
- 230000008025 crystallization Effects 0.000 claims abstract description 7
- 239000011780 sodium chloride Substances 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 85
- 238000003860 storage Methods 0.000 claims description 54
- 239000007788 liquid Substances 0.000 claims description 47
- 239000012452 mother liquor Substances 0.000 claims description 34
- 238000000926 separation method Methods 0.000 claims description 32
- 239000000126 substance Substances 0.000 claims description 24
- 230000006835 compression Effects 0.000 claims description 23
- 238000007906 compression Methods 0.000 claims description 23
- 239000003921 oil Substances 0.000 claims description 23
- 239000003814 drug Substances 0.000 claims description 14
- 238000007667 floating Methods 0.000 claims description 13
- 238000004062 sedimentation Methods 0.000 claims description 13
- 239000002562 thickening agent Substances 0.000 claims description 13
- 238000011282 treatment Methods 0.000 claims description 13
- 238000005189 flocculation Methods 0.000 claims description 12
- 230000016615 flocculation Effects 0.000 claims description 12
- 238000010992 reflux Methods 0.000 claims description 12
- 238000004140 cleaning Methods 0.000 claims description 9
- 239000008399 tap water Substances 0.000 claims description 9
- 235000020679 tap water Nutrition 0.000 claims description 9
- 238000005119 centrifugation Methods 0.000 claims description 8
- 238000003672 processing method Methods 0.000 claims description 7
- 239000013078 crystal Substances 0.000 claims description 6
- 229940079593 drug Drugs 0.000 claims description 6
- 230000008719 thickening Effects 0.000 claims description 6
- 239000000084 colloidal system Substances 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 238000000605 extraction Methods 0.000 claims description 4
- 238000007790 scraping Methods 0.000 claims description 4
- 239000002893 slag Substances 0.000 claims description 4
- 230000008676 import Effects 0.000 claims description 3
- 239000004615 ingredient Substances 0.000 claims description 3
- 238000002844 melting Methods 0.000 claims description 3
- 230000008018 melting Effects 0.000 claims description 3
- 238000010025 steaming Methods 0.000 claims 2
- 238000004065 wastewater treatment Methods 0.000 abstract description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 abstract description 3
- 230000003311 flocculating effect Effects 0.000 abstract description 2
- 239000010842 industrial wastewater Substances 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 22
- 239000000243 solution Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 239000005416 organic matter Substances 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 238000000053 physical method Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000005345 coagulation Methods 0.000 description 2
- 230000015271 coagulation Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 230000001376 precipitating effect Effects 0.000 description 2
- 229920002545 silicone oil Polymers 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 238000002207 thermal evaporation Methods 0.000 description 2
- JPVYNHNXODAKFH-UHFFFAOYSA-N Cu2+ Chemical compound [Cu+2] JPVYNHNXODAKFH-UHFFFAOYSA-N 0.000 description 1
- 239000012028 Fenton's reagent Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- PTFCDOFLOPIGGS-UHFFFAOYSA-N Zinc dication Chemical compound [Zn+2] PTFCDOFLOPIGGS-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 229910001431 copper ion Inorganic materials 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000003487 electrochemical reaction Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000006056 electrooxidation reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000001802 infusion Methods 0.000 description 1
- 229920000592 inorganic polymer Polymers 0.000 description 1
- 229910000765 intermetallic Inorganic materials 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000011859 microparticle Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- LPUQAYUQRXPFSQ-DFWYDOINSA-M monosodium L-glutamate Chemical compound [Na+].[O-]C(=O)[C@@H](N)CCC(O)=O LPUQAYUQRXPFSQ-DFWYDOINSA-M 0.000 description 1
- 235000013923 monosodium glutamate Nutrition 0.000 description 1
- 239000004223 monosodium glutamate Substances 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229920000620 organic polymer Polymers 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 230000032696 parturition Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C01D3/04—Chlorides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/043—Details
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- 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
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- 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
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- 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
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
-
- 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
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- 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
- C02F1/5281—Installations for water purification using chemical 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
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- 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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/29—Chlorine compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
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- Chemical & Material Sciences (AREA)
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- 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)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a kind of organic silicon wastewater processing system and methods, belong to industrial waste water treatment.Its system includes Wastewater Pretreatment unit, one effect evaporation element, two effect evaporation elements, steam circulation unit and desalination unit, wherein, Wastewater Pretreatment unit, one effect evaporation element, two effect evaporation elements and desalination unit are sequentially connected, organic silicon wastewater stoste is separated through desalination unit after an effect evaporation element and two effect evaporation element evaporative crystallizations after Wastewater Pretreatment unit flocculating setting and is centrifuged, and the secondary steam that an effect evaporation element and two effect evaporation elements generate is recycled by steam circulation unit, effectively reduce power consumption and steam economy, chloride ion content is low in treated waste water simultaneously, and 95% or more sodium chloride content in the salinity solid isolated, it is alternatively arranged as Nacl reuse.
Description
Technical field
The present invention relates to industrial waste water treatments, and in particular to a kind of organic silicon wastewater processing system and side
Method.
Background technique
Organosilicon has the title of " industrial monosodium glutamate ", is widely used in every field.It can be generated in its production process a certain amount of
Waste water, have the characteristics that high COD, high salt, grease layering are unobvious, and complicated components, containing gas chromatography, inorganic
Metallic compound, and also containing heavy metals chemical combination such as a certain amount of Adsorbable organic halogens, silica gel, copper ion, zinc ions
Object.
Since organic silicon wastewater is many kinds of, complicated component, biodegradability is poor, and pH value is very low, is in highly acid, and toxicity is big,
Containing contents of many kinds of heavy metal ion, discharge of wastewater fluctuation is big, and regularity is poor.Due to these problems, the work so that wastewater treatment is got up
Skill is complicated, and route is long, and processed waste water is difficult to qualified discharge.
Currently, the processing technique of organic silicon wastewater specifically includes that both at home and abroad
1, physical method: the processing of Typical physical method mainly includes mixing, flocculation, precipitating, filtering etc., due in organic silicon wastewater
Pollutant component is complicated, and the organic matter of mostly bio-refractory, brings certain difficulty to the processing of organic silicon wastewater.
2, chemical oxidization method: chemical oxidization method can handle a variety of hardly degraded organic substances under normal temperature and pressure conditions, solve
Some polymer and long-chain molecule are difficult to the problem of degrading, so that organic silicon wastewater is centainly handled.
3, stripping process technology: air- extraction is directly to be contacted by vapor with waste water, keeps the volatility in waste water organic
Object is diffused into gas phase, and pollutant is separated from waste water.
In physical method, also need to select suitable medicament to guarantee coagulating sedimentation according to water quality property in coagulation process
Effect, since change of water quality is big, treatment effect change greatly.In chemical oxidization method, H in the Fenton reagent that uses2O2Use
It is lower to measure larger and utilization rate, Fe2+Need to just it stablize in the solution system that pH is 2.5~3.0, it is desirable that it is harsh, and the processing work
The problems such as skill can also generate a large amount of sludge, and operating cost greatly increases.Stripping process technology and microelectrolysis processing technical treatment
Load is lower, can not meet the wastewater flow rate of organosilicon generation.
In addition, there are also microelectrolysis processing technology and biochemical processing other than above-mentioned processing technique, micro-electrolysis method is
Pretreated technique is carried out to the difficult waste water of biology using the electrochemical corrosion principle of metal, primary battery is constituted using iron, charcoal,
Electrochemical reaction occurs, but microelectrolysis processing technology exclusive use effect is poor, is not suitable for being used alone.And since organosilicon is useless
Water biodegradability is poor, and less about Study on Biochemical Treatment, is difficult to realize industrialize now.
Summary of the invention
The purpose of the present invention is to provide a kind of organic silicon wastewater processing system and methods, to solve existing industrial treatment
The problem of organic silicon wastewater, can by waste water the dregs of fat and chloride ion effectively remove, the salinity in waste water can be recycled, through handling
Waste water energy afterwards is recycled and is just discharged after up to standard.
The technical scheme to solve the above technical problems is that
A kind of organic silicon wastewater processing system, including Wastewater Pretreatment unit, one effect evaporation element, two effect evaporation elements,
Steam circulation unit and desalination unit,
The input terminal and output end of one effect evaporation element are single with the output end of Wastewater Pretreatment unit and two effect evaporations respectively
The output end of the input terminal connection of member, two effect evaporation elements is connect with the input terminal of desalination unit；The mother liquor reflux of desalination unit
Outlet is connected to the mother liquor reflux entrance of two effect evaporation elements by pipeline, and the mother liquor for desalination unit to be centrifugated out returns
It is back to two effect evaporation elements；
The steam gas outlet of one effect evaporation element and two effect evaporation elements by the steam of pipeline and steam circulation unit into
Port connection, and evaporation elements are imitated with an effect evaporation element and two respectively by pipeline in the steam gas outlet of steam circulation unit
Steam entry port connection, the secondary steam for generating an effect evaporation element and two effect evaporation elements are defeated through steam circulation unit
It send into an effect evaporation element and two effect evaporation elements.
Further, in preferred embodiments of the present invention, above-mentioned Wastewater Pretreatment unit include water reservoir, oil separation tank,
Air floatation machine, the medicine system connecting with air floatation machine and the pond connecting with an effect evaporation element, the outlet of oil separation tank and water store up
The entrance in pond connects, and the outlet of water reservoir is connected by the entrance of air bearing elevator pump and air floatation machine, the outlet and pond of air floatation machine
Entrance connection；
Medicine system includes that the PAC chemicals dosing plant, PAM chemicals dosing plant and concentrated base connecting respectively with the dosing mouth of air floatation machine add
Medicine device.
Further, in preferred embodiments of the present invention, above-mentioned organic silicon wastewater processing system, which is characterized in that
One effect evaporation element includes that storage of waste water tank and the 1st effective evaporator and one connecting with two effect evaporation elements imitate separator,
The entrance of storage of waste water tank is connected by the outlet in waste water delivery pump and pond, and the outlet of storage of waste water tank and one
Imitate the bottom end entrance connection of evaporator；The bottom end outlet of 1st effective evaporator is entered by the top of an effect circulating pump and 1st effective evaporator
Mouth connection, is evaporated for returning to the evaporation liquid in 1st effective evaporator in 1st effective evaporator；The bottom end of 1st effective evaporator
Outlet is also connect with two effect evaporation elements by an effect circulating pump, for the evaporation liquid after 1st effective evaporator separates to be sent to two
Imitate evaporation element condensing crystallizing；The bottom end outlet of one effect separator is connected to by pipeline with the bottom end outlet of 1st effective evaporator.
Further, in preferred embodiments of the present invention, above-mentioned two effects evaporation elements include 2nd effect evaporator and
Two effect separators being connect with desalination unit,
Bottom end outlet of the entrance of two effect separators by an effect circulating pump and an effect separator, the bottom end of two effect separators
Outlet is connected by the bottom end entrance of two effect circulating pumps and 2nd effect evaporator, the top export of 2nd effect evaporator and two effect separators
Bottom end entrance connection.
Further, in preferred embodiments of the present invention, above-mentioned desalination unit includes thickener, centrifuge and mother liquor
Tank,
The entrance of thickener is connect by two effect discharging pumps with the discharge port of two effect separators, the outlet and centrifugation of thickener
The import of machine connects, and the solid outlet of centrifuge is by fixed conveyor band connection, the liquid outlet of centrifuge and mother liquor tank
The mother liquor reflux outlet of entrance connection, mother liquor tank is connect with the mother liquor reflux entrance of 2nd effect evaporator.
Further, in preferred embodiments of the present invention, above-mentioned steam circulation unit includes vapour compression machine, and steam
Compressor is MVR vapour compression machine,
One effect separator steam (vapor) outlet and two effect separators steam (vapor) outlet respectively with the steam inlet of vapour compression machine
Connection, the steam (vapor) outlet of vapour compression machine connect with the steam inlet of 1st effective evaporator and the steam inlet of 2nd effect evaporator respectively
It connects.
Further, in preferred embodiments of the present invention, above-mentioned organic silicon wastewater processing system further includes cleaning condensation
Unit, cleaning condensing unit include preheater, plate-type condenser, the first water condensate storage tank, the second water condensate storage tank, condensation
Water pump and vacuum pump, preheater are arranged between storage of waste water tank and 1st effective evaporator；
Ejected wash water or tap water are entered by the cleaning that pipeline is connected to storage of waste water tank, an effect separator and two effect separators
Mouthful,
1st effective evaporator, 2nd effect evaporator condensation-water drain be connected to the first water condensate storage tank, vapour compression machine
Condensation-water drain is connected to the second water condensate storage tank, and the second water condensate storage tank is connected to the first water condensate storage tank；The
One water condensate storage tank is connected to by condensate pump with preheater；
The noncondensable gas outlet of 1st effective evaporator, 2nd effect evaporator is connected by the entrance of pipeline and plate-type condenser,
The fixed gas outlet of plate-type condenser is connect with the entrance of vacuum pump.
The processing method of above-mentioned organic silicon wastewater processing system, comprising:
(1) being transported to Wastewater Pretreatment unit to adjust pH value by organic silicon wastewater stoste is progress dosing flocculation after neutrality
Processing；
(2) stoste after Wastewater Pretreatment cell processing is transported in an effect evaporation element after being exchanged heat by preheater and adds
Thermal evaporation concentration, then it is transported to evaporative crystallization in two effect evaporation elements；
(3) the isolated magma of two effect evaporation elements is transported to separate after thickening in desalination unit and is centrifuged, centrifugation point
From Solid Conveying and Melting go out and mother liquor after being centrifuged is transported in two effect evaporation elements；
The secondary steam that (4) one effect evaporation elements and two effect evaporation elements generate is by defeated after the extraction compression of steam circulation unit
It is sent in an effect evaporation element and two effect evaporation elements；
(5) ejected wash water or tap water are transported to storage of waste water tank, an effect separator and two effect separators and clean to it；
The noncondensable gas in secondary steam is generated to 1st effective evaporator and 2nd effect evaporator by plate-type condenser to condense, wherein
Fixed gas in noncondensable gas is then extracted out by vacuum pump.
Further, in preferred embodiments of the present invention, the processing method of above-mentioned organic silicon wastewater processing system is special
Sign is, comprising:
(1) by organic silicon wastewater stoste by oil separation tank by sedimentation carry out floating oil collecting after, after entering in water reservoir
It is sent in air floatation machine by pipeline, is added after the concentrated base chemicals dosing plant adjusting pH value to neutrality in medicine system, then through PAC
Medicine device and PAM chemicals dosing plant flocculate；Wherein, upper layer floating object scrapes through the Slag Scraping Device in air floatation machine and is delivered to sludge-tank,
Subnatant is sent to an effect evaporation element；Upper layer floating object includes elaioleucite, suspended matter or colloid substances in waste water；
(2) be sent to after the preheated device heat exchange preheating of subnatant in air floatation machine 1st effective evaporator be evaporated it is dense
Contracting, the bottom evaporation liquid evaporated through 1st effective evaporator returns to be recycled at the top of 1st effective evaporator through an effect circulating pump to be steamed
Hair concentration；The bottom obtained through 1st effective evaporator evaporation liquid is delivered in an effect separator and carries out gas-liquid separation；One effect separation
The separating liquid that device is isolated is pumped into two effect evaporation elements through an effect circulation, and the secondary steam body that an effect separator is isolated is sent to
Steam circulation unit；Wherein, the bottom evaporation liquid that 1st effective evaporator obtains can be pumped into two effect evaporation elements by an effect circulation；
(3) the bottom evaporation liquid from 1st effective evaporator or the separating liquid in an effect separator are sent to two effect separators
Gas-liquid separation again isolates liquid by pipeline and is sent in 2nd effect evaporator evaporative crystallization again, obtains in 2nd effect evaporator
Evaporated on top liquid return to gas-liquid separation in two effect separators again, the magma that two effect separators are isolated is sent to desalination unit,
The secondary steam that two effect separators are isolated is sent to steam circulation unit；
(4) magma from two effect separators, which is sent in thickener, to be thickened, and the magma after thickening is delivered to centrifugation
Solid-liquid centrifugation separation is carried out in machine, the crystal being centrifuged out transfers out, and the centrifuge mother liquor being centrifuged out enters mother liquor tank, returns again to
It is sent in 2nd effect evaporator；Wherein the ingredient of crystal is mainly solid sodium chloride；
(5) through compressing after the secondary steam in an effect separator and two effect separators is sent in steam compressor
Back to being recycled in the 1st effective evaporator and the 2nd effect evaporator；
(6) ejected wash water or tap water are sent to respectively in an effect separator and two effect separators, and are being sent to an effect separator
When also pass through storage of waste water tank；
(7) noncondensable gas in 1st effective evaporator and 2nd effect evaporator generation secondary steam is sent to board-like cold by pipeline
It is condensed in condenser, fixed gas therein is sent in fixed gas tank and is extracted out again by vacuum pump；
1st effective evaporator and 2nd effect evaporator generate the condensed water in secondary steam and are sent to the storage of the first condensed water by pipeline
Tank is deposited, the condensed water that vapour compression machine generates is then sent through in the first water condensate storage tank after being first sent to the second water condensate storage tank,
Condensed water is sent to preheater by pipeline and carries out heat exchange with the subnatant in air floatation machine in first water condensate storage tank
After be discharged.
Further, in preferred embodiments of the present invention, the range of pH value is 6-8 in above-mentioned steps (1)；Flocculation treatment
Condition be: the PAC that solution concentration is 10% is added, additional amount accounts for the 5-15% of wastewater volume；Solution concentration, which is added, is
0.5% PAM, additional amount account for the 0.1-0.5% of wastewater volume；1st effective evaporator and 2nd effect evaporator in step (2) and (3)
The temperature for the secondary steam isolated is 90-92 DEG C.
The present invention carries out continuous treatment to waste water, first waste water is placed in oil separation tank isolate float on the surface on it is free
The dregs of fat, then be transported in air floatation machine first carry out acid-base neutralization adjust pH to 6-8, add efficient flocculant PAC and PAM, make
Flocculation reaction occurs for organic matter in waste water and PAC and PAM, at this moment the floating material in waste water and colloid substances react to be formed it is big
Floating " alumen ustum floc sedimentation " under the intensive air bubble buoyancy effect that release of the chemistry floc sedimentation in air floatation machine generates, floats rapidly
Liquid level is scraped by the scraper plate in air floatation machine and is excreted into sludge conveyer.And the bigger suspended matter of minute quantity specific gravity in waste water
It is then sunk to rapidly in the groove body in air floatation machine in precipitating cone, is concentrated and is passed through outside the regular device for transferring of valve naturally.
It can not be filtered containing a large amount of oil and thin particulate matter since oil and grain diameter are too thin in organic silicon wastewater, and
It can not settle for a long time.If the method for taking absorption, it will generate a large amount of micro- waste, uneconomical environmental protection, and grasped for interval
Make, large labor intensity is not suitable for large batch of wastewater treatment.Therefore selective flocculation method, joint utilize flocculant PAC and PAM, adopt
PAC is inorganic polymer flocculant, and PAM is organic polymer coargulator, and PAC flocculating effect is good, but alumen ustum is broken；And PAM
Coagulation aiding is played, the alumen ustum that PAC can be allowed to be formed, which is polymerized to bulk, to be helped to precipitate.To make oil and fine particle in waste water flocculate
It is agglomerating under the action of agent, it is settled after agglomerating slowly, the gas absorption generated using air floatation machine reduces the close of floc sedimentation on floc sedimentation
Degree, and then make on floc sedimentation quickly bubbles through the water column is scraped by Slag Scraping Device and flow to sludge-tank into the equipment slot that grafts clay, effectively removed thin in waste water
Microparticle evaporates desalination for waste water and provides good water quality, reduce waste water with continuous treatment and reduction amount of scale buildup can by steam
Consumption.
To waste water by flocculation sedimentation processing after, be evaporated except salt treatment, mainly by one effect evaporation element,
Two effect evaporation elements, desalination unit, steam circulation unit and cleaning unit utilize an effect evaporation element in steam circulation unit
The low temperature position secondary steam generated with two effect evaporation element evaporations converts electric energy to thermal energy after vapour compression machine is extracted out, this
It is the temperature and pressure raising of steam, heat content increases, and then re-enters into an effect evaporation element and two effect evaporation elements, sufficiently
Using latent heat of the steam, wastewater treatment liquid is made to maintain fluidized state.The steam to be discarded originally is set just to be fully utilized,
Latent heat has been recycled, the thermal efficiency is improved, the economy for theoretically giving birth to steam is equivalent to 30 effects of multiple-effect evaporation, reduces sewage treatment
Steam energy consumption, processing cost is lower, has saved most infusion of financial resources and operating cost.
The invention has the following advantages:
Organic silicon wastewater is first first carried out oil removal and flocculation sedimentation processing by the present invention, is first isolated free on floating on the surface
The dregs of fat after using the organic matter in flocculant PAC and PAM and waste water flocculation sedimentation occurs under the action of air floatation machine, then into
Row evaporation removes salt treatment, and the secondary steam of generation is recycled by steam circulation unit, effectively reduces power consumption and steam
Consumption.Using organic silicon wastewater processing system of the invention, chloride ion content can drop in waste water after processing
200ppm is hereinafter, COD value is 400-500ppm；95% or more sodium chloride content in salinity solid after processing, water content 4% with
Under, it can be used as Nacl reuse.And every evaporation ton water power consumption is less than 43KWh, steam economy is less than 25kg.
Detailed description of the invention
Fig. 1 is organic silicon wastewater processing system structural block diagram of the invention；
Fig. 2 is the structure chart of organic silicon wastewater processing system of the invention；
Fig. 3 is the enlarged drawing in the portion A in Fig. 2；
Fig. 4 is the enlarged drawing in the portion B in Fig. 2；
Fig. 5 is the enlarged drawing in the portion C in Fig. 2.
In Fig. 2-5: 101- water reservoir；102- oil separation tank；103- air floatation machine；104-PAC chemicals dosing plant；105-PAM dosing
Device；106- concentrated base chemicals dosing plant；The pond 107-；108- air bearing elevator pump；109- waste water delivery pump；201- storage of waste water tank；
202- 1st effective evaporator；203- mono- imitates separator；204- mono- imitates circulating pump；301- 2nd effect evaporator；302- bis- imitates separator；
303- bis- imitates circulating pump；304- waste water discharging pump；401- thickener；402- centrifuge；403- mother liquor tank；404- Recycling Mother Solution
Pump；501- vapour compression machine；601- preheater；602- plate-type condenser；603- the first water condensate storage tank；604- second is condensed
Water store tank；605- condensate pump；606- vacuum pump.
Specific embodiment
The principle and features of the present invention will be described below with reference to the accompanying drawings, and the given examples are served only to explain the present invention, and
It is non-to be used to limit the scope of the invention.
Embodiment
Please refer to Fig. 1, organic silicon wastewater processing system of the invention, including Wastewater Pretreatment unit, an effect evaporation element,
Two effect evaporation elements, steam circulation unit and desalination unit,
The input terminal and output end of one effect evaporation element are single with the output end of Wastewater Pretreatment unit and two effect evaporations respectively
The output end of the input terminal connection of member, two effect evaporation elements is connect with the input terminal of desalination unit；The mother liquor reflux of desalination unit
Outlet is connected to the mother liquor reflux entrance of two effect evaporation elements by pipeline, and the mother liquor for desalination unit to be centrifugated out returns
It is back to two effect evaporation elements；
Steam is connect by pipeline with the steam inlet of an effect evaporation element, an effect evaporation element and two effect evaporation elements
Steam gas outlet connect with the steam inlet of steam circulation unit by pipeline, and the steam gas outlet of steam circulation unit
By pipeline respectively with one effect evaporation element and two effect evaporation elements steam entry port connect, for by one effect evaporation element with
The secondary steam that two effect evaporation elements generate is through in steam circulation unit transportation to an effect evaporation element and two effect evaporation elements.
Referring to figure 2. and Fig. 3, Wastewater Pretreatment unit include water reservoir 101, oil separation tank 102, air floatation machine 103 and air bearing
The medicine system and pond 107, the outlet of oil separation tank 102 that machine 103 connects are connect with the entrance of water reservoir 101, water reservoir 101
Outlet connect with the entrance of air floatation machine 103 by air bearing elevator pump 108, the outlet of air floatation machine 103 and the entrance company in pond 107
It connects；
Medicine system includes the PAC chemicals dosing plant 104 connecting respectively with the dosing mouth of air floatation machine 103, PAM chemicals dosing plant
105 and concentrated base chemicals dosing plant 106.
Referring to figure 2. and Fig. 4, an effect evaporation element include storage of waste water tank 201,1st effective evaporator 202 and an effect separation
Device 203,
The entrance of storage of waste water tank 201 is connect by waste water delivery pump 109 with the outlet in pond 107, and storage of waste water tank
201 outlet is connect with the bottom end entrance of 1st effective evaporator 202；The bottom end outlet of 1st effective evaporator 202 passes through an effect circulating pump
204 connect with the top inlet of 1st effective evaporator 202, for evaporating the evaporation liquid in 1st effective evaporator 202 back to an effect
It is repeatedly evaporated in device 202；The bottom end of 1st effective evaporator 202 is connected to the bottom end of an effect separator 203.
Referring to figure 2. and Fig. 5, two effect evaporation elements include 2nd effect evaporator 301 and two effect separators 302, two effect separation
The entrance of device 302 is connect by an effect circulating pump 204 with the bottom end outlet of an effect separator 203；The bottom end of two effect separators 302
Outlet by two effect circulating pumps 303 connect with the bottom end entrance of 2nd effect evaporator 301, the top export of 2nd effect evaporator 301 and
The bottom end entrance connection of two effect separators 302.
Referring to figure 2. and Fig. 5, desalination unit includes thickener 401, centrifuge 402 and mother liquor tank 403, thickener 401
Entrance is connect by two effect discharging pumps 304 with the discharge port of two effect separators 302, outlet and the centrifuge 402 of thickener 401
Import connection, and the solid outlet of centrifuge 402 passes through fixed conveyor band connection, the liquid outlet and mother liquor tank of centrifuge 402
The mother liquor reflux outlet of 403 entrance connection, mother liquor tank 403 is connect with the mother liquor reflux entrance of 2nd effect evaporator 301.
Referring to figure 2. and Fig. 5, steam circulation unit includes vapour compression machine 501, and vapour compression machine 501 is MVR steam
Compressor,
Steam is connected to by pipeline with the steam inlet of 1st effective evaporator 202, the steam (vapor) outlet and two of an effect separator 203
The steam (vapor) outlet of effect separator 302 is connect with the steam inlet of vapour compression machine 501 respectively, and the steam of vapour compression machine 501 goes out
Mouth is connect with the steam inlet of the steam inlet of 1st effective evaporator 202 and 2nd effect evaporator 301 respectively.
Referring to figure 2., Fig. 4 and Fig. 5, organic silicon wastewater processing system further include cleaning condensing unit, clean condensing unit
Including preheater 601, plate-type condenser 602, the first water condensate storage tank 603, the second water condensate storage tank 604, condensate pump
605 and vacuum pump 606, preheater 601 is arranged between storage of waste water tank 201 and 1st effective evaporator 202；
Ejected wash water or tap water are connected to storage of waste water tank 201, one by pipeline and imitate separator 203 and two effect separators
302 cleaning entrance, 1st effective evaporator 202,2nd effect evaporator 301 condensation-water drain be connected to the first water condensate storage tank
603, the condensation-water drain of vapour compression machine 501 is connected to the second water condensate storage tank 604, and the second water condensate storage tank 604
It is connected to the first water condensate storage tank 603；First water condensate storage tank 603 is connected to by condensate pump 605 with preheater 601；
The noncondensable gas outlet of 1st effective evaporator 202,2nd effect evaporator 301 passes through pipeline and plate-type condenser 602
The fixed gas outlet of entrance connection, plate-type condenser 602 is connect with the entrance of vacuum pump 606.
The processing method of organic silicon wastewater processing system of the invention, comprising:
(1) being transported to Wastewater Pretreatment unit to adjust pH value by organic silicon wastewater stoste is progress dosing flocculation after neutrality
Processing；
(2) stoste after Wastewater Pretreatment cell processing is transported in an effect evaporation element after being exchanged heat by preheater and adds
Thermal evaporation concentration, then it is transported to evaporative crystallization in two effect evaporation elements；
(3) the isolated magma of two effect evaporation elements is transported to separate after thickening in desalination unit and is centrifuged, centrifugation point
From Solid Conveying and Melting go out and mother liquor after being centrifuged is transported in two effect evaporation elements；
The secondary steam that (4) one effect evaporation elements and two effect evaporation elements generate is by defeated after the extraction compression of steam circulation unit
It is sent in an effect evaporation element and two effect evaporation elements；
(5) ejected wash water or tap water are transported to storage of waste water tank, an effect separator and two effect separators and clean to it；
The noncondensable gas in secondary steam is generated to 1st effective evaporator and 2nd effect evaporator by plate-type condenser to condense, wherein
Fixed gas in noncondensable gas is then extracted out by vacuum pump.
Further, in preferred embodiments of the present invention, the processing method of above-mentioned organic silicon wastewater processing system, packet
It includes:
(1) by organic silicon wastewater stoste by oil separation tank by sedimentation carry out floating oil collecting after, after entering in water reservoir
It is sent in air floatation machine by pipeline, is added after the concentrated base chemicals dosing plant adjusting pH value to neutrality in medicine system, then through PAC
Medicine device and PAM chemicals dosing plant flocculate；Wherein, upper layer floating object scrapes through the Slag Scraping Device in air floatation machine and is delivered to sludge-tank,
Subnatant is sent to an effect evaporation element；Upper layer floating object includes elaioleucite, suspended matter or colloid substances in waste water；
(2) be sent to after the preheated device heat exchange preheating of subnatant in air floatation machine 1st effective evaporator be evaporated it is dense
Contracting, the bottom evaporation liquid evaporated through 1st effective evaporator returns to be recycled at the top of 1st effective evaporator through an effect circulating pump to be steamed
Hair concentration；The bottom obtained through 1st effective evaporator evaporation liquid is delivered in an effect separator and carries out gas-liquid separation；One effect separation
The separating liquid that device is isolated is pumped into two effect evaporation elements through an effect circulation, and the secondary steam body that an effect separator is isolated is sent to
Steam circulation unit；Wherein, the bottom evaporation liquid that 1st effective evaporator obtains can be pumped into two effect evaporation elements by an effect circulation；
(3) the bottom evaporation liquid from 1st effective evaporator or the separating liquid in an effect separator are sent to two effect separators
Gas-liquid separation again isolates liquid by pipeline and is sent in 2nd effect evaporator evaporative crystallization again, obtains in 2nd effect evaporator
Evaporated on top liquid return to gas-liquid separation in two effect separators again, the magma that two effect separators are isolated is sent to desalination unit,
The secondary steam that two effect separators are isolated is sent to steam circulation unit；
(4) magma from two effect separators, which is sent in thickener, to be thickened, and the magma after thickening is delivered to centrifugation
Solid-liquid centrifugation separation is carried out in machine, the crystal being centrifuged out transfers out, and the centrifuge mother liquor being centrifuged out enters mother liquor tank, returns again to
It is sent in 2nd effect evaporator；Wherein the ingredient of crystal is mainly solid sodium chloride；
(5) through compressing after the secondary steam in an effect separator and two effect separators is sent in steam compressor
Back to being recycled in the 1st effective evaporator and the 2nd effect evaporator；
(6) ejected wash water or tap water are sent to respectively in an effect separator and two effect separators, and are being sent to an effect separator
When also pass through storage of waste water tank；
(7) noncondensable gas in 1st effective evaporator and 2nd effect evaporator generation secondary steam is sent to board-like cold by pipeline
It is condensed in condenser, fixed gas therein is sent in fixed gas tank and is extracted out again by vacuum pump；
1st effective evaporator and 2nd effect evaporator generate the condensed water in secondary steam and are sent to the storage of the first condensed water by pipeline
Tank is deposited, the condensed water that vapour compression machine generates is then sent through in the first water condensate storage tank after being first sent to the second water condensate storage tank,
Condensed water is sent to preheater by pipeline and carries out heat exchange with the subnatant in air floatation machine in first water condensate storage tank
After be discharged.
Further, in preferred embodiments of the present invention, the range of pH value is 6,7,8 in above-mentioned steps (1), preferably pH
Value is 7；The condition of flocculation treatment is: be added solution concentration be 10% PAC, additional amount account for wastewater volume 5%, 10%,
15%, preferably 10%；Be added solution concentration be 0.5% PAM, additional amount account for wastewater volume 0.1%, 0.3%,
0.5%, preferably 0.3%.The temperature for the secondary steam that 1st effective evaporator and 2nd effect evaporator are isolated in step (2) and (3)
For 90 DEG C, 91 DEG C, 92 DEG C, preferably 91 DEG C.
Wherein, the general main source of organic silicon wastewater in step (1) is deep de- waste water, water scrubber waste water, alkali-wash waste water
With containing hydrogen silicone oil waste water, deeply de- waste water, water scrubber waste water, alkali-wash waste water wherein not oil-containing need not move through oil separation tank can be direct
It is sent in water reservoir, and oil-containing is then sent through water storage after then needing to first pass through oil separation tank sedimentation, floating oil collecting in containing hydrogen silicone oil waste water
Chi Zhong.Waste water in water reservoir is sent in air floatation machine.
The foregoing is merely presently preferred embodiments of the present invention, is not intended to limit the invention, it is all in spirit of the invention and
Within principle, any modification, equivalent replacement, improvement and so on be should all be included in the protection scope of the present invention.
Claims (10)
1. a kind of organic silicon wastewater processing system, which is characterized in that including Wastewater Pretreatment unit, an effect evaporation element, two effects
Evaporation element, steam circulation unit and desalination unit,
It is described one effect evaporation element input terminal and output end respectively with the output end of the Wastewater Pretreatment unit and described two
The input terminal connection of evaporation element is imitated, the output end of the two effects evaporation element is connect with the input terminal of the desalination unit；Institute
The mother liquor reflux outlet for stating desalination unit is connected to the mother liquor reflux entrance of the two effects evaporation element by pipeline, is used for institute
It states the mother liquor that desalination unit is centrifugated out and is back to the two effects evaporation element；
The steam gas outlet of the one effect evaporation element and the two effects evaporation element passes through pipeline and the steam circulation unit
Steam inlet connection, and the steam gas outlet of the steam circulation unit by pipeline respectively with it is described one effect evaporation element
It is connected with the steam entry port of the two effects evaporation element, for generate an effect evaporation element and two effect evaporation elements
Secondary steam is through steam circulation unit transportation into an effect evaporation element and the two effects evaporation element.
2. organic silicon wastewater processing system according to claim 1, which is characterized in that the Wastewater Pretreatment unit includes
Water reservoir (101), oil separation tank (102), air floatation machine (103), the medicine system being connect with the air floatation machine (103) and with it is described
The pond (107) of one effect evaporation element connection, the outlet of the oil separation tank (102) are connect with the entrance of the water reservoir (101),
The outlet of the water reservoir (101) is connect by air bearing elevator pump (108) with the entrance of the air floatation machine (103), the air bearing
The outlet of machine (103) is connect with the entrance of the pond (107)；
The medicine system includes that PAC chemicals dosing plant (104), the PAM connecting respectively with the dosing mouth of the air floatation machine (103) add
Medicine device (105) and concentrated base chemicals dosing plant (106).
3. organic silicon wastewater processing system according to claim 2, which is characterized in that the effect evaporation element includes useless
Water store tank (201) and 1st effective evaporator (202) the He Yixiao separator (203) being connect with the two effects evaporation element,
The entrance of the storage of waste water tank (201) is connect by waste water delivery pump (109) with the outlet of the pond (107), and
The outlet of the storage of waste water tank (201) is connect with the bottom end entrance of the 1st effective evaporator (202)；The 1st effective evaporator
(202) bottom end outlet is connect by effect circulating pump (204) with the top inlet of the 1st effective evaporator (202), and being used for will
Evaporation liquid in the 1st effective evaporator (202), which returns in the 1st effective evaporator (202), to be evaporated；The one effect evaporation
The bottom end outlet of device (202) is also connect with the two effects evaporation element by effect circulating pump (204), for that will evaporate through an effect
Evaporation liquid after device (202) separation is sent to two effect evaporation element condensing crystallizings；The bottom end outlet of one effect separator (203) is logical
Piping is connected to the bottom end outlet of the 1st effective evaporator (202).
4. organic silicon wastewater processing system according to claim 3, which is characterized in that the two effects evaporation element includes two
Effect evaporator (301) and two effects separator (302) being connect with the desalination unit,
The bottom end outlet of the entrance of two effect separator (302) and effect separator (203), the two effects separator
(302) bottom end outlet is connect by two effects circulating pump (303) with the bottom end entrance of the 2nd effect evaporator (301), and described two
The top export for imitating evaporator (301) is connect with the bottom end entrance of two effect separator (302).
5. organic silicon wastewater processing system according to claim 4, which is characterized in that the desalination unit includes thickener
(401), centrifuge (402) and mother liquor tank (403),
The entrance of the thickener (401) is connected by the discharge port of two effects discharging pump (304) and two effect separator (302)
It connects, the outlet of the thickener (401) is connect with the import of the centrifuge (402), and the solid of the centrifuge (402) goes out
Mouth is connect by fixed conveyor band connection, the liquid outlet of the centrifuge (402) with the entrance of the mother liquor tank (403), institute
The mother liquor reflux outlet for stating mother liquor tank (403) is connect with the mother liquor reflux entrance of the 2nd effect evaporator (301).
6. organic silicon wastewater processing system according to claim 5, which is characterized in that the steam circulation unit includes steaming
Vapour compressor (501), and the vapour compression machine (501) is MVR vapour compression machine,
It is described one effect separator (203) steam (vapor) outlet and it is described two effect separator (302) steam (vapor) outlet respectively with the steaming
The steam inlet of vapour compressor (501) connects, the steam (vapor) outlet of the vapour compression machine (501) respectively with the 1st effective evaporator
(202) steam inlet is connected with the steam inlet of the 2nd effect evaporator (301).
7. organic silicon wastewater processing system according to claim 1-6, which is characterized in that the organic silicon wastewater
Processing system further includes cleaning condensing unit, and the cleaning condensing unit includes preheater (601), plate-type condenser (602), the
One water condensate storage tank (603), the second water condensate storage tank (604), condensate pump (605) and vacuum pump (606), the preheating
Device (601) is arranged between the storage of waste water tank (201) and the 1st effective evaporator (202)；
It is separator (203) and described that ejected wash water or tap water by pipeline are connected to the storage of waste water tank (201), an effect
The cleaning entrance of two effects separator (302),
The 1st effective evaporator (202), the 2nd effect evaporator (301) condensation-water drain be connected to the first water condensate storage tank
(603), the condensation-water drain of the vapour compression machine (501) is connected to the second water condensate storage tank (604), and described second cold
Condensate holding vessel (604) is connected to the first water condensate storage tank (603)；The first water condensate storage tank (603) passes through
Condensate pump (605) is connected to the preheater (601)；
The 1st effective evaporator (202), the 2nd effect evaporator (301) noncondensable gas outlet by pipeline with it is described board-like
The entrance of condenser (602) connects, the entrance of the fixed gas outlet and the vacuum pump (606) of the plate-type condenser (602)
Connection.
8. the processing method of organic silicon wastewater processing system according to claim 7 characterized by comprising
(1) being transported to Wastewater Pretreatment unit to adjust pH value by organic silicon wastewater stoste is progress dosing flocculation treatment after neutrality；
(2) stoste after Wastewater Pretreatment cell processing is transported to heat in an effect evaporation element after exchanging heat by preheater and steam
Hair concentration, then it is transported to evaporative crystallization in two effect evaporation elements；
(3) the isolated magma of two effect evaporation elements is transported to separate after thickening in desalination unit and is centrifuged, centrifuge separation
Mother liquor after Solid Conveying and Melting goes out and is centrifuged is transported in two effect evaporation elements；
The secondary steam that (4) one effect evaporation elements and two effect evaporation elements generate after the extraction compression of steam circulation unit by being transported to
In one effect evaporation element and two effect evaporation elements；
(5) ejected wash water or tap water are transported to storage of waste water tank, an effect separator and two effect separators and clean to it；Pass through
Plate-type condenser generates the noncondensable gas in secondary steam to 1st effective evaporator and 2nd effect evaporator and condenses, wherein non-cold
Fixed gas in solidifying gas is then extracted out by vacuum pump.
9. the processing method of organic silicon wastewater processing system according to claim 8 characterized by comprising
(1) by organic silicon wastewater stoste by oil separation tank by sedimentation carry out floating oil collecting after, pass through after entering in water reservoir
Pipeline is sent in air floatation machine, is filled after the concentrated base chemicals dosing plant adjusting pH value to neutrality in medicine system, then through PAC dosing
It sets and flocculates with PAM chemicals dosing plant；Wherein, upper layer floating object scrapes through the Slag Scraping Device in air floatation machine and is delivered to sludge-tank, lower layer
Clear liquid is sent to an effect evaporation element；Upper layer floating object includes elaioleucite, suspended matter or colloid substances in waste water；
(2) subnatant in air floatation machine through condensation water preheater heat exchange preheating after be sent to 1st effective evaporator be evaporated it is dense
Contracting, the bottom evaporation liquid evaporated through 1st effective evaporator returns to be recycled at the top of 1st effective evaporator through an effect circulating pump to be steamed
Hair concentration；The bottom obtained through 1st effective evaporator evaporation liquid is delivered in an effect separator and carries out gas-liquid separation；One effect separation
The separating liquid that device is isolated is pumped into two effect evaporation elements through an effect circulation, and the secondary steam body that an effect separator is isolated is sent to
Steam circulation unit；Wherein, the bottom evaporation liquid that 1st effective evaporator obtains can be pumped into two effect evaporation elements by an effect circulation；
(3) the bottom evaporation liquid from 1st effective evaporator or the separating liquid in an effect separator are sent to two effect separators again
Gas-liquid separation isolates liquid by pipeline and is sent in 2nd effect evaporator evaporative crystallization again, pushes up obtained in 2nd effect evaporator
Portion's evaporation liquid returns to gas-liquid separation in two effect separators again, and the magma that two effect separators are isolated is sent to desalination unit, two effects
The secondary steam that separator is isolated is sent to steam circulation unit；
(4) magma from two effect separators, which is sent in thickener, to be thickened, and the magma after thickening is delivered in centrifuge
Solid-liquid centrifugation separation is carried out, the crystal being centrifuged out transfers out, and the centrifuge mother liquor being centrifuged out enters mother liquor tank, returns again to and is sent to
In 2nd effect evaporator；Wherein the ingredient of crystal is mainly solid sodium chloride；
(5) it is returned after the secondary steam in an effect separator and two effect separators is sent in steam compressor through compression
It is recycled into the 1st effective evaporator and the 2nd effect evaporator；
(6) ejected wash water or tap water are sent to respectively in an effect separator and two effect separators, and also when being sent to an effect separator
By storage of waste water tank；
(7) noncondensable gas that 1st effective evaporator and 2nd effect evaporator generate in secondary steam is sent to plate-type condenser by pipeline
Middle condensation, fixed gas therein are sent in fixed gas tank and are extracted out again by vacuum pump；
The condensed water that 1st effective evaporator and 2nd effect evaporator generate in secondary steam is sent to the first water condensate storage tank by pipeline,
The condensed water that vapour compression machine generates is then sent through in the first water condensate storage tank after being first sent to the second water condensate storage tank, and first is cold
Condensed water is sent to after preheater carries out heat exchange with the subnatant in air floatation machine by pipeline and is discharged in condensate holding vessel.
10. the processing method of organic silicon wastewater processing system according to claim 9, which is characterized in that pH in step (1)
The range of value is 6-8；The condition of flocculation treatment is: the PAC that solution concentration is 10% is added, additional amount accounts for the 5- of wastewater volume
15%；The PAM that solution concentration is 0.5% is added, additional amount accounts for the 0.1-0.5% of wastewater volume；One in step (2) and (3)
The temperature for the secondary steam that effect evaporator and 2nd effect evaporator are isolated is 90-92 DEG C.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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| CN113200577A (en) * | 2021-05-29 | 2021-08-03 | 苏州美田环保科技有限公司 | MVR evaporation system for wastewater recovery |
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