CN107162301A - Cutting fluid recovery and processing system and processing method - Google Patents
Cutting fluid recovery and processing system and processing method Download PDFInfo
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- CN107162301A CN107162301A CN201710404278.9A CN201710404278A CN107162301A CN 107162301 A CN107162301 A CN 107162301A CN 201710404278 A CN201710404278 A CN 201710404278A CN 107162301 A CN107162301 A CN 107162301A
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- 238000012545 processing Methods 0.000 title claims abstract description 59
- 239000002173 cutting fluid Substances 0.000 title claims abstract description 29
- 238000011084 recovery Methods 0.000 title claims abstract description 22
- 238000003672 processing method Methods 0.000 title claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 185
- 238000001914 filtration Methods 0.000 claims abstract description 48
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 44
- 238000005189 flocculation Methods 0.000 claims abstract description 35
- 230000016615 flocculation Effects 0.000 claims abstract description 35
- 239000002699 waste material Substances 0.000 claims abstract description 23
- 238000000034 method Methods 0.000 claims abstract description 22
- 230000003647 oxidation Effects 0.000 claims abstract description 9
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 9
- 208000001840 Dandruff Diseases 0.000 claims abstract description 4
- 239000002253 acid Substances 0.000 claims description 64
- 239000002351 wastewater Substances 0.000 claims description 50
- 238000000926 separation method Methods 0.000 claims description 34
- 239000007789 gas Substances 0.000 claims description 31
- 230000018044 dehydration Effects 0.000 claims description 26
- 238000006297 dehydration reaction Methods 0.000 claims description 26
- 239000007788 liquid Substances 0.000 claims description 24
- 230000009183 running Effects 0.000 claims description 14
- 238000006555 catalytic reaction Methods 0.000 claims description 11
- 239000000463 material Substances 0.000 claims description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 9
- 239000012528 membrane Substances 0.000 claims description 9
- 238000006386 neutralization reaction Methods 0.000 claims description 9
- 230000008569 process Effects 0.000 claims description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 8
- 239000002585 base Substances 0.000 claims description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 8
- 230000008859 change Effects 0.000 claims description 7
- 238000012544 monitoring process Methods 0.000 claims description 7
- 238000004065 wastewater treatment Methods 0.000 claims description 7
- 239000012153 distilled water Substances 0.000 claims description 6
- 230000005611 electricity Effects 0.000 claims description 6
- 230000008676 import Effects 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 239000000498 cooling water Substances 0.000 claims description 5
- 238000013461 design Methods 0.000 claims description 5
- 229910052751 metal Inorganic materials 0.000 claims description 5
- 239000002184 metal Substances 0.000 claims description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 4
- 230000015572 biosynthetic process Effects 0.000 claims description 4
- 229910052742 iron Inorganic materials 0.000 claims description 4
- 239000003344 environmental pollutant Substances 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 231100000719 pollutant Toxicity 0.000 claims description 3
- 150000003384 small molecules Chemical class 0.000 claims description 3
- 206010020843 Hyperthermia Diseases 0.000 claims description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 2
- 238000005253 cladding Methods 0.000 claims description 2
- 238000005345 coagulation Methods 0.000 claims description 2
- 230000015271 coagulation Effects 0.000 claims description 2
- 239000012141 concentrate Substances 0.000 claims description 2
- 230000001351 cycling effect Effects 0.000 claims description 2
- 238000004821 distillation Methods 0.000 claims description 2
- 239000003574 free electron Substances 0.000 claims description 2
- 230000036031 hyperthermia Effects 0.000 claims description 2
- 229920002521 macromolecule Polymers 0.000 claims description 2
- 235000015927 pasta Nutrition 0.000 claims description 2
- 239000002957 persistent organic pollutant Substances 0.000 claims description 2
- 239000002893 slag Substances 0.000 claims description 2
- 239000002002 slurry Substances 0.000 claims description 2
- 230000001360 synchronised effect Effects 0.000 claims description 2
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims 3
- 210000000481 breast Anatomy 0.000 claims 1
- 239000002975 chemoattractant Substances 0.000 claims 1
- 230000001105 regulatory effect Effects 0.000 claims 1
- 230000010148 water-pollination Effects 0.000 claims 1
- 238000005520 cutting process Methods 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 3
- 239000012530 fluid Substances 0.000 abstract 1
- 230000009471 action Effects 0.000 description 24
- 239000003814 drug Substances 0.000 description 13
- 238000005273 aeration Methods 0.000 description 8
- 239000000126 substance Substances 0.000 description 8
- 239000002360 explosive Substances 0.000 description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 238000001704 evaporation Methods 0.000 description 6
- 230000008020 evaporation Effects 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
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- 230000002045 lasting effect Effects 0.000 description 2
- 238000005461 lubrication Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 229910021645 metal ion Inorganic materials 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000011120 plywood Substances 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 230000007017 scission Effects 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 101100278884 Arabidopsis thaliana E2FD gene Proteins 0.000 description 1
- 101100278886 Arabidopsis thaliana E2FF gene Proteins 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 206010020741 Hyperpyrexia Diseases 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 101100187186 Solanum lycopersicum LE16 gene Proteins 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
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- 238000004220 aggregation Methods 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 238000003556 assay Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 210000005056 cell body Anatomy 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
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- 230000008021 deposition Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009300 dissolved air flotation Methods 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 238000004945 emulsification Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hcl hcl Chemical compound Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 229910000000 metal hydroxide Inorganic materials 0.000 description 1
- 150000004692 metal hydroxides Chemical class 0.000 description 1
- 238000003801 milling Methods 0.000 description 1
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- 238000012986 modification Methods 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000010525 oxidative degradation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000002161 passivation Methods 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011002 quantification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000009738 saturating Methods 0.000 description 1
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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
- 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
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
Abstract
The invention discloses cutting fluid recovery and processing system, including four stage processing systems, the four stages processing system includes first stage processing system, second stage processing system, phase III processing system and the fourth stage processing system once connected by pump, and the method for cutting fluid recycling comprises the following steps：Anti-dandruff oil removing；MVR is demulsified and recuperation of heat；Electric flocculation oxidation and the water-oil separating of condensed water；Micro-pipe filtering, reverse osmosis filtering and UV oxidations, make cutting waste fluid be down to below 100PPM from high concentration COD (concentration average out to 150,000PPM).
Description
Technical field
The present invention relates to industrial wastes processing technology field, more particularly to cutting fluid recovery and processing system and processing method.
Background technology
First, evolution
Simple Lathe industry, numerically controlled lathe industry, milling machine industry, machine finishing industry and tool processes industry etc., due to producing in the industry
Take specification bigger, part industry is when working process metal appearance, and lathe used is fast due to mechanical rotating shaft rotating speed, in car
Bed drill bit is with processed material surface because hyperpyrexia occurs for friction, and industry uses cutting fluid and is injected into lathe drill bit and machined object
Surface reaches the purpose of cooling, lubrication, cleaning and antirust, so that wherein cutting fluid and chip turn into major pollutants.By
In being cooled to cut main purpose, therefore in the configuration of cutting fluid composition, water account for about 90~95% ratios, and in order to there is the work(of lubrication
Can, grease is again inevitable, and water oil allotment dissolving, interfacial agent also into one of important factor, when cutting fluid in itself
When excessively polluting and can not purify recycling in simple mechanical filter mode, cutting fluid must work as groove and give up to avoid damaging quilt
The surface of workpiece and as waste product.
When being discarded due to the cutting fluid used in finishing industry, COD tails assay is about 100,000~200,
000PPM。
2nd, combustion method
Conjunction rule discharge is handled in the discharge (100,000~200,000PPM of COD concentration) of the such high concentration of waste water
(below COD100PPM), the method that typically can effectively use imports all waste water in waste water incinerator to incinerate, to burn
Mode be it is simplest, it is most fast, but cause environment secondary (air) pollution be also need solve.
3rd, electric flocculation method
Electric flocculation method is by Absorptive complex wave and redox, acid-base neutralization, dissolved air flotation knot by electric flocculation method of iron or aluminium
Waste water treatment process altogether；This method is that the flocculant of positively charged and contaminant particle are passed through into electrostatic attraction and Fan Dewa
Power, complexing aggregation is agglomerating, generates the floccule body that can be settled and removes, organic molecule can resolve into small molecule by anodic oxidation
(chemical bond is oxidized scission of link) and be easy to be flocculated agent absorption, the metal ion of dyestuff and solubilised state then can be by the electricity of negative electrode also
Former deposition is separated with water body, when waste water is in alkalescence, and the metal ion that Anodic Stripping is produced is consumed through hydrolysis and complexing
Excessive OH-, declines pH in waste water；And for acid waste water, the OH- energy that metal hydroxides and cathodic electrolytic water are produced
H+ in waste water is consumed, pH is increased, thus, electric flocculation plays the role of to neutralize soda acid.In addition, when formation such as processing oily waste waters
When the micro- light, hardly possible of flco is settled, also using cathode hydrogen evolution or the follow-up electric floating technique of coupling, the O produced by electrolysis water2And H2It is (straight
Footpath is no more than 60 μm, much smaller than pressurization bubble diameter) micro- light flco is brought to the water surface in floating-upward process reach separation purpose, and
The process is without the reagents such as outer throwing PAM and processing flocculation sludge.Electric floating also has the function that certain electroxidation removes COD concurrently.Electricity
Flocculence is a complicated materialization technology, and its core content is the generation of flocculant.When in electrolyte contain Cl-When be conducive to electricity
Flocculence handles waste water, Cl-It can be generated with strong oxidizing property and Bleachability Cl in anode2And HClO, can be by the organic matter in water
Oxidative degradation, and remove colourity；Simultaneously as Cl-Radius is small, penetration capacity is strong, be easily adsorbed in anode and with metal formation can
Soluble compound, therefore the passivating film perforation rupture of electrode surface can be made, accelerate the dissolving of metal passivation layer.
Due to electric flocculation method, high COD concentration is highly effective in processes, but processing ultrahigh concentration COD (100,000~
200000PPM) during waste water, removal ability still can not (100PPM) up to standard, processing completion about 20,000~40,000PPM.
4th, MVR (Mechanical Vapor Recomposition) (mechanical vapor recompression)
MVR is mechanical steam recompression technology (mechanical vapor recompression) abbreviation, is profit
The indirect steam and its energy produced with vapo(u)rization system itself, high-order is promoted to by mechanical work of the steam of low order through compressor
Steam source.So return to vapo(u)rization system and heat energy is provided, so as to reduce a power-saving technology of the demand of the energy to external world.
MVR is forced back to evaporator by heater, separator and is forced back to pump etc. and constitutes.Material is changed in the heat exchanger tube of heat exchanger
Steam heating-up temperature rise outside heat pipe, in the case where returning to pumping action, material is risen in separator.Evaporation produce indirect steam from
Overflowed in material, material is concentrated generation supersaturation and makes crystalline growth, and the oversaturated material of releasing, which enters, is forced back to pump,
Return and enter heat exchanger under pumping action, material, which is so returned, to be constantly concentrated by evaporation or condensing crystallizing.In crystallization and evaporation separator
Indirect steam is transported to compressor after the separator purification on vapor seperator top, after compressor compresses indirect steam
It is transported to heat exchanger shell pass and heats steam as evaporator, realizes that heat energy returns to continuous evaporation.
Because MVR is concentrated by evaporation inorganic substances quite effectively (after concentration crystallize), but the material based on the organic hydrophilic base
Then still can not effectively it be fully solved；Organic water soluble COD (COD, ring work contaminated wastewater index) (or it may be said that
For BOD (biochemical oxygen demand (BOD), ring work contaminated wastewater index)), can be by COD when the body surface of localized contact Pistonless compressor
Switch to VOC (VOC, ring work exhaust emission index), and be dissolved in vapor, cause vapor liquid equilibrium phenomenon, with
The discharge of distilled water and discharge.So that for the processing of groove cutting liquid, COD concentration of emissions still have about 5,000~10,000PPM
(about 95% clearance), can not still pass through discharging standards.
The content of the invention
To overcome disadvantages mentioned above, the present invention for basic handling mode, makes cutting with " MVR- electric flocculations-RO-UV oxidations "
Waste liquid is down to below 100PPM from high concentration COD (concentration average out to 150,000PPM) processing.
In order to reach object above, the technical solution adopted by the present invention is：Cutting fluid recovery and processing system, including four stages
Processing system, the four stages processing system includes first stage processing system, the second stage processing being sequentially connected by pump
System, phase III processing system and fourth stage processing system；
The first stage processing system takes off including passing sequentially through the adjustment tank-I of acid and alkali-resistance pneumatic diaphragm pump connection, scum silica frost
Water dispenser-I, collecting tank-I, adjustment tank-II and adjustment tank-III, are provided with oil removing between the adjustment tank-II and the adjustment tank-III
Device；
The second stage processing system is returned including MVR rapid steamers, circulating slot, oil-water separation tank, collecting tank-II and waste oil
Groove is received, the MVR rapid steamers pass through water pump formation inner loop, the MVR rapid steamers and the profit point with the circulating slot
Connected from groove by pipeline, the oil-water separation tank is connected with the collecting tank-II by pipeline, the collecting tank-II and institute
Waste oil accumulator tank is stated to connect by pipeline, the waste oil accumulator tank with it is legal recovery waste oil groove be connected, the oil-water separation tank and
Between the collecting tank-II, acid and alkali-resistance pneumatic diaphragm pump is set between the collecting tank-II and the waste oil accumulator tank；
The phase III processing system include be sequentially connected adjustment tank-IV, acidifying groove, collecting tank-III, adjustment tank-
Vth, electric flocculation machine, adjustment tank-VI, alkalization groove, collecting tank-IV, adjustment tank-VII, dross dehydration machine-II and collecting tank-V, institute
State between adjustment tank-IV and the acidifying groove, between the collecting tank-III and the adjustment tank-V, the adjustment tank-VI with
Between the alkalization groove, the collecting tank-IV and the adjustment tank-VII, the adjustment tank-VII and the dross dehydration machine-II
Provided with acid and alkali-resistance pneumatic diaphragm pump, working barrel is set between the adjustment tank-V and the electric flocculation machine；
The fourth stage processing system includes passing sequentially through the adjustment tank-VIII of high-pressure pump connection, micro-pipe filter, adjustment
Groove-Ⅸ, reverse osmosis filter, adjustment tank-Ⅹ, backwash tank, UV catalysis grooves-I and UV catalysis groove-II, the micro-pipe filter
Neutralization chamber, collecting tank-VI are set gradually between the adjustment tank-Ⅸ, the UV catalysis grooves-II pass through acid and alkali-resistance with releasing chute
Pneumatic diaphragm pump is connected, and is used to reclaim waste water energy, reverse osmosis processing is added in the most back segment of wastewater treatment, in order to protect
The usage cycles of reverse osmosis membrane, in adding micro-pipe filter before reverse osmosis, because the waste water filtering ratio of reverse osmosis is 7：3, such as
This low treatment effect causes cost for wastewater treatment to greatly improve, to make wastewater treatment into reduction, so that in the system design
It can more be received and be saved, the system has added two-period form reverse osmosis equipment to improve efficiency, and total amount waste water filtering ratio is 9：
1；
The acid and alkali-resistance pneumatic diaphragm pump is connected by five mouthfuls of two valves with air compressor machine.
Further, the MVR rapid steamers include MVR rapid steamers-I and MVR rapid steamer-II, the MVR rapid steamers-I and
MVR rapid steamers-II are in parallel, and the oil-water separation tank includes oil-water separation tank-I and oil-water separation tank-II, the water-oil separating
Groove-I and oil-water separation tank II are in parallel, and the oil-water separation tank-I and oil-water separation tank-II pass through pipeline and the adjustment respectively
Groove-I is connected.
Further, the electric flocculation machine includes electric flocculation machine-I and electric flocculation machine-II, and the electric flocculation machine-I and electricity are wadded a quilt with cotton
Solidifying machine-II is in parallel.
Further, the micro-pipe filter includes micro-pipe filter-I and micro-pipe filter-II, the micro-pipe filtering
Device-I and micro-pipe filter-II are in parallel, and the micro-pipe filter-I and micro-pipe filter-II connect with the adjustment tank-VII respectively
Connect, the micro-pipe filter-I and micro-pipe filter-II are connected with the backwash tank respectively, and the reverse osmosis filter includes
Reverse osmosis filter-I, reverse osmosis filter-II and reverse osmosis filter-III, the reverse osmosis filter-I, reverse osmosis filtering
Machine-II and reverse osmosis filter-III are connected with the backwash tank by high-pressure pump respectively, the reverse osmosis filter-I, inverse
Filter-II and reverse osmosis filter-III is penetrated to be connected with the adjustment tank-I respectively.
Further, the collecting tank-I, oil-water separation tank, collecting tank-II, waste oil accumulator tank and collecting tank-V are set
Digital level meter, the liquid level for monitoring pasta and liquid level, the adjustment tank-I, adjustment tank-II, adjustment tank-III, adjustment
Groove-IV, adjustment tank-V, adjustment tank-VI, adjustment tank-VII, adjustment tank-VIII, adjustment tank-Ⅸ, adjustment tank-Ⅹ, oil-water separation tank,
Liquid level gauge is set on circulating slot, collecting tank-III, collecting tank-IV, collecting tank-VI and releasing chute, the acidifying groove, alkalization groove, in
Set PH to count with groove, mixer is set in the acidifying groove, alkalization groove and the neutralization chamber.
Further, the adjustment tank-I, adjustment tank-II, adjustment tank-III, adjustment tank-IV, adjustment tank-V, adjustment tank-
VIth, adjustment tank-VII, adjustment tank-VIII, adjustment tank-Ⅸ, adjustment tank-Ⅹ, UV catalysis grooves-I and UV catalysis grooves-II pass through gas respectively
Body pipeline valve is connected with air blower.
Further, between the MVR rapid steamers and the circulating slot, the MVR rapid steamers and the oil-water separation tank
Between, motor-driven valve, the backwash tank and the micro-pipe filter are set between the oil-water separation tank and the collecting tank-II
Between motor-driven valve is set.
Further, the electric flocculation machine uses tubular type electric flocculation machine.
The method of cutting fluid recycling comprises the following steps：
(1) anti-dandruff oil removing：Metal scraps in waste liquid and oil slick are removed by the way that dross dehydration machine-I and oil expeller are preliminary；
(2) MVR demulsifications and recuperation of heat：During MVR, localized hyperthermia causes organic emulsified base molecular changes property, its
Middle emulsification molecular hydrophylic is destroyed, and is temporarily stored into as water-oil separating material in concentrate, in addition, steam compressed process because of
High temperature causes organic molecule to become VOC and is partially soluble in vapor, is liquefied as distillate with vapor and discharges outside MVR,
Due to causing COD pollutants to discharge therewith containing VOC in water distillation, the long key of macromolecule being not easily decomposed due to the VOC category of discharge
Carbon/phenyl ring type organic pollutant, while MVR equipment operations, because compressor operation can discharge substantial amounts of heat simultaneously
Source, is cooled down by running water and reclaimed；
MVR equipment a total of two is entered four and gone out：
Two enter：High-concentration waste water to be processed is needed to enter；Pistonless compressor cooling cycling use of water enters；
Four go out：High pollution condensed water is discharged；Hyperthermal distilled water treats that after-treatment waste water is discharged；Recirculated cooling water is discharged；It is low
Warm steam discharge；
(3) electric flocculation oxidation and the water-oil separating of condensed water：Condensed water due to hydrophilic group and long key carbon after demulsifying phenomenon and/
Or phenyl ring class scission of link, wherein long key carbon molecules shows the characteristic of oil molecule, floating is automatically separated because profit is incompatible, is gone out
Existing water-oil separating phenomenon, upper strata oil is recyclable, and lower floor's oily waste water and waste residue are back to initial waste groove；
Waste water after MVR is handled enters adjustment tank, first adjusts pH value with hydrochloric acid, and wastewater electrolytic matter is increased with synchronous,
Electric flocculation machine is imported with working barrel again, now the ring-type carbon key in waste water and long key carbon molecules are because of the oxidability of conductive electric energy
As simple small molecule organic pollution, adding the cladding coagulation for producing hydrogen-oxygen ferrous iron with anode iron makes pollution molecular change
Effectively filtering is able to greatly to remove；
(4) micro-pipe filtering and reverse osmosis filtering
Used to reclaim waste water energy, reverse osmosis processing is added in the most back segment of wastewater treatment, in order to protect reverse osmosis
The usage cycles of film, in adding micro-pipe filter before reverse osmosis；
(5) UV is aoxidized
Because waste water still suffers from micro peculiar smell after the completion of processing, aoxidized in system end plus UV catalysis grooves,
Ozone free electron base being produced, COD is also can remove except can remove stink.
Further, two layers above and below being formed after the discharge of the concentration of high pollution described in step (2) waste water because of demulsification, upper strata is
Recyclable oil, lower floor is water and bits slag, and circulation imports in raw wastewater pond and refilters processing.
Further, hyperthermal distilled water described in step (2) is imported in adjustment tank after after the discharge of after-treatment waste water, regulation
Water quality and water treat that next stage is handled.
Further, the discharge of recirculated cooling water described in step (2) Posterior circle is used, in circulating water chennel, more than setting
Temperature can be supplied as slurry.
Cutting fluid recovery and processing system and method that the present invention is provided, cutting fluid is handled to country's discharge in waste water mode
It is below the mark to be discharged, without combustion system, chemical agent (demulsifier and flocculant) is not used yet, and only with micro acid
And alkali, suitable cost is saved actually, and as environmental protection and energy saving subtract another performance of carbon.
Brief description of the drawings
Fig. 1 is embodiments of the invention structured flowchart.
In figure：
Embodiment
Presently preferred embodiments of the present invention is described in detail below in conjunction with the accompanying drawings, so that advantages and features of the invention energy
It is easier to be readily appreciated by one skilled in the art, apparent is clearly defined so as to be made to protection scope of the present invention.
Referring to shown in accompanying drawing 1, cutting fluid recovery and processing system and processing method in the present embodiment, including
First, first stage-anti-dandruff oil removing
1. acted before system boot
The T09 of circulating slot-I and the T10 of circulating slot-II are filled to high water level with running water；Again by releasing chute T28 water fillings repeatedly
To explosive barrel D04；So that D02 and D04 bubble medicines are completed.
2. steep medicine
With manually opened pipeline valve V23, shutoff valve V22, pump P28 is under " ON " state by recycle-water in releasing chute T28
(REC WATER) (it is anhydrous in releasing chute when system is operated for the first time, replace coming into operation to total system with running water producing back
Receive water.) be delivered in explosive barrel D04, pump P28 " OFF " when high water level；By in quantification tablet alkali input explosive barrel D04；Now, bucket
Interior temperature monitoring meter TE03 schedules 60 DEG C (can be adjusted with man-machine design), during more than design temperature, and system high temperature moves report action, stops
Only offer medicine, when temperature drop to 40 DEG C (can be adjusted with man-machine setting) (moving report to notify), offer medicine again to quantitative and complete (fixed
It is 5000KG that amount, which refers to addition water, and piece alkali is 5000KG, is brewed to 50%, the NaOH solution of proportion 1.52).
The NaOH solution soaked is injected into explosive barrel D02 to high level with chemicals feeder C04, now, previous step is repeated, by medicine
Bucket D04 bubble medicines are completed.
Steep medicine and adjustment system blower A01, A02 or A03 are opened that (three spare unit each other, are used alternatingly simultaneously.) explosive barrel
The gas piping valve AV21 of top is opened, and bubble medicine completes manual-lock.
If explosive barrel D02 is when low liquid level, issue " explosive barrel low liquid level moves report ", to notify operating personnel to carry out bubble medicine work,
When operating personnel carry out bubble medicine, shifting report switch can be closed in a manual manner.
3. water inlet
Open system, system blower totally three (two is standby with one), air blower automatically turns on wherein two when " automatic "
Platform, in setting time then, it is automatic alternately wherein one (time was defined by three hours, can by man-machine setting it).Now, adjust
Water-level gauge LE01 in the whole T01 of groove-I monitors that the water-level gauge LE02 in high water level, the T03 of adjustment tank-II monitors non-ultrahigh water
Position, acid and alkali-resistance pneumatic diaphragm pump P01, which starts, injects waste water in dross dehydration machine K01 until liquid level gauge LE02 reaches surcharge water level
And or liquid level gauge LE01 reach low water level when, pump stopping action (the water quantity monitoring meter FM1 of acid and alkali-resistance pneumatic diaphragm pump " P01 " afterwards
For flow monitoring).
This water inlet action adjoint system air blower is opened and gas piping valve " AV01 "~" AV10 " is opened so that waste water fills
Part stirring mixing；When pump stopping is acted, pipeline valve " AV01 "~" AV10 " is closed.
Be " automatic " mode above, operating personnel can " manual " (manual type) operate each details (to be generally tentatively
Used during Shi Commissioning), arrestment is acted when " stopping ".
4. dross dehydration machine is filtered
The dross dehydration machine used in filtering designed by this stage is K01, and the acid and alkali-resistance membrane pump of correspondence is P01, correspondence
Filtered water collection groove-I be T02, the liquid level in corresponding groove is calculated as " DLE1 " (digital level meter), the filtering completion water of correspondence
Delivery pump is " P02 ".
In setting dross dehydration machine " manual ", " automatic " and " stopping " in control panel, herein different from " filtration system " institute
Its " manual ", " automatic " and " stopping " are set, the behaviour whether dross dehydration machine is " manual ", " automatic " or " stopping " in itself is referred exclusively to herein
Make.
System is when progress is filtered, and lasting aeration to filtration is completed in the T01 of adjustment tank-I, the setting of filtration pressure
In 6KG/CM2.(in aeration time-histories, gas piping valve " AV01 "~" AV10 " is opened.)
" manual ", " automatic " and " stopping " may be selected in dross dehydration machine K01, and when " manual ", filter pressure is in 6KG/CM2It is lower and
Filtering completes water no longer water outlet and continues more than 5 minutes, represents dross dehydration machine filtering time-histories and has completed, now filtrate is full, stops
Only acid and alkali-resistance pneumatic diaphragm pump P01 action, (dross dehydration machine it) conveyer action, oil hydraulic cylinder release of pressure opens sheet frame, scum silica frost
Filtrate (because of gravity) is unloaded automatically, is transported to hopper by (dross dehydration machine it) conveyer and (is transported to discarded object stockpile manually
Abandoned with to be shipped), oil hydraulic cylinder send pressure, and sheet frame plywood, acid and alkali-resistance pneumatic diaphragm pump P01 actions continue to filter.
During dewaterer " automatic ", " PP01 " gauge pressure continues 6KG/CM2More than (can be adjusted with man-machine setting), corresponding receipts
Collect liquid level gauge DLE1 in the T02 of groove-I, every 10 minutes (can be by man-machine setting) liquid level difference is no more than 1 centimeter, and plate and frame dewaterer is certainly
The dynamic program for completing above-mentioned " manual ".
When dross dehydration machine is set in " stopping ", maintenance shut-downs.
When filtration system carries out " automatic ", start acid and alkali-resistance pneumatic diaphragm pump P01, filtering completes water and enters collecting tank-I
Set liquid level gauge " DLE1 " control acid and alkali-resistance pneumatic diaphragm pump " P02 " " skyer ", water when 50 centimeters of height of water level in T02, groove
Position 10 centimeters " low to stop " of height.
When filtration system carries out " manual ", each equipment and the manually opened test of pipeline valve.
5. oil removing
Filtering complete water be stored in the T03 of adjustment tank-II until water-level gauge LE02 when high water level, acid and alkali-resistance membrane pump P03
When " automatic ", automatic start keeps in high water level to treat next step through oil expeller E01 to the T04 of adjustment tank-III.
2nd, second stage-MVR demulsifications, recuperation of heat and oily-water seperating equipment
Before 1.MVR actions
When MVR (" automatic ") starts, PLC automatically confirms that two work (in before MVR initial actuatings) completions；First, following
The T09 of annular groove-I or ring follow one of the T10 of groove-II tank for full-water level, and, the circulation work water pump P 08 of correspondence or P10 operations
In；Second, in the T05 of oil-water separation tank-I or T06 of oil-water separation tank-II operations, and, one of valve V13 or valve V14 of correspondence
For in opening.
2.MVR demulsifications, recuperation of heat and oily-water seperating equipment
The two of MVR enter and four go out to be described below：
Two enter：
Recirculated water part, if during the K02 of MVR rapid steamers-I unlatchings, now PLC confirm in advance the T09 of circulating slot-I and circulating slot-
Water temperature whichever in II T10 is higher, if temperature it is more a height of the former, the circulating slot of running is the T09 of circulating slot-I, now circulating-water valve
V03 and V05 are opened, if in addition, during the K03 of MVR rapid steamers-II unlatchings, circulating-water valve V08 and V10 are opened, working barrel P09 Kai Qi
Make；Conversely, then with the T10 of circulating slot-II operate, working barrel P11 running, will originally water circulation squeeze into the K02 of MVR rapid steamers-I and/
Or the K03 of MVR rapid steamers-II synchronously starts the circulating-water valve of correspondence.
If when the temperature monitoring meter TE01 in the T09 of circulating slot-I monitors water temperature more than more than 50 DEG C, opening acid and alkali-resistance gas
Dynamic membrane pump P10, by high-temperature water drainage in groove to circulating hot water reclaiming system, in addition, alternately another back-up system, change by circulating slot-
II T10 is operated, now, closes cycle bleeder valve V05 and/or V10, ON cycle drain valve V04 and/or V09, and cycle bleeder
Valve V03 and/or V08 keep original state, and notify working barrel P10 runnings simultaneously, will be circulated in acid and alkali-resistance pneumatic diaphragm pump P09
When hot water in the T09 of groove-I is expelled to water-level gauge LE06 " low water level ", acid and alkali-resistance pneumatic diaphragm pump P09 decommissions, running water
Untill water compensating valve V12 is opened into water-level gauge LE06 high water level, now, the work of MVR circulating coolings is alternately the T10 of circulating slot-II
Operation；After one section of time-histories, the temperature monitoring meter TE02 in the T10 of circulating slot-II is more than 50 DEG C, alternately to another circulating slot, relatively
The step answered is ibid.
Waste water part, it is automatic to start MVR evaporations if the T04 of adjustment tank-III water-level gauge LE03 is when high water level (" HI ")
The K02 of machine-I, it is in parallel during surcharge water level (" HI-HI ") to start another K03 of MVR evaporators-II, when low water level (" LO "), stop
The only K03 of MVR evaporators-II, when ultra low water level (" LO-LO "), the K02 of MVR rapid steamers-I stops, when high water level next time,
Starting another, (two alternate-runnings, superelevation parallel running, one stopping of low water level, ultra low water level two is all to stop state.).
Four go out：
High pollution condensed water is discharged, and the concentration waste water that MVR is discharged, its COD is at a relatively high, belongs to high pollution, and come because polluting
Source is different, and the oil molecule of the composition containing different proportion is floated on above waste water, system when running, PLC Auto-Sensings oil-water separation tank-
I T05 water-level gauge DEL2 and the T06 of oil-water separation tank-II water-level gauge DEL3 whichever trough inner water position are higher and do not belong to high water level, then
The pipeline valve of groove top is V13 or V14 " ON ", and high pollution condensed water is expelled to after corresponding groove, one section of time-histories, the groove full-water level
Afterwards, the valve that is discharged into of upper square groove is closed, and the pipeline valve of another groove is opened, and high pollution condensed water is discharged into, and two grooves are used alternatingly；In system
When initial, the T05 of default oil-water separation tank-I is initial slot, top pipeline valve V13 " ON ", until liquid level gauge DLE2 in groove
When " HI ", pipeline valve V13 " OFF ", now, and another groove, the T10 of oil-water separation tank-II alternately catcher runnings, pipeline valve V14 " ON ",
It is discharged into containing high pollution condensed water is received, untill high water level；In addition, the T05 of oil-water separation tank-I starts to be counted by PLC when high water level
When, after three hours (can by man-machine setting it), acid and alkali-resistance pneumatic diaphragm pump P04 " ON ", until water level in the T05 of oil-water separation tank-I
LE05 " LO ", acid and alkali-resistance pneumatic diaphragm pump P04 " OFF " are counted, if oil reservoir height (can be set more than 100 centimeters by man-machine in this time slot
It is fixed it) (surveyed by water-level gauge DLE2 detect height deduct water-level gauge LE05 low liquid levels highly obtain it), now pipeline valve V15 and acid and alkali-resistance
Pneumatic diaphragm pump P06 " ON " is until oil reservoir highly stops oil extraction action, pipeline valve V15 and acid and alkali-resistance pneumatic diaphragm less than 20 centimeters
Pump P06 " OFF ", when alternately being acted to another groove, when tankful, repeats this step.Water-level gauge DLE4 in collecting tank -2T07
During for " HI ", start acid and alkali-resistance pneumatic diaphragm pump P07 until trough inner water position meter DLE4 stops when being " LO "；Waste oil accumulator tank T08
Notify that reclaiming dealer comes to reclaim waste oil when interior water-level gauge DLE5 is " HI ", now, acid and alkali-resistance pneumatic diaphragm pump P08 is with " hand
It is dynamic " mode extracts waste oil in waste oil accumulator tank T08 to low water level.
When the water-level gauge LE08 that hyperthermal distilled water is expelled in the T11 of adjustment tank-IV, groove is " HI ", acid and alkali-resistance pump gas is notified
Dynamic membrane pump P13 actions, when water-level gauge LE08 is " LO ", acid and alkali-proof pump pneumatic diaphragm pump P13 stoppings action, trough inner water position meter
When LE08 is " HI-HI ", the K03 stoppings of-I K02 and MVR rapid steamers of MVR rapid steamers-II action in all runnings.
Action detailed " two enter " its " recirculated water " part of recirculated cooling water discharge.
Low-temperature steam is discharged, when working barrel P09 is acted, when the K02 of MVR rapid steamers-I works, and pipeline valve V02 " ON ", MVR steams
When the K03 of hair machine-II works, pipeline valve V07 " ON ", low-temperature steam imports the T09 of circulating slot-I；Conversely, during working barrel P11 actions,
When the K02 of MVR rapid steamers-I works, pipeline valve V01 " ON ", when the K03 of MVR rapid steamers-II works, pipeline valve V06 " ON ", low temperature steams
Conductance enters the T10 of circulating slot-II.
3rd, phase III-waste water acidifying, electric flocculation oxidation, waste water alkalization and filtering
1. waste water is acidified
Palpus enough conducting electrolytes when passing through electric flocculation due to waste water, wherein being preferred with chloride ion-containing, in wastewater treatment
It is optimal selection that hydrochloric acid (HCl) acidifying is added in processing procedure, and acid and alkali-resistance pneumatic diaphragm pump P13 is in water-level gauge in the T11 of adjustment tank-IV
Start during LE08 " HI ", interlock the M01 of mixer-I and carry out waste water stirring, it is now, adjoint in the chemicals feeder C01 in acidifying groove T12
Dosing, and chemicals feeder when (can in it is set on ph controller), be stopped less than 4 with ph controller PH01 control waste water qualities
C01 is acted.Skyer is low stops by water water-level gauge LE09 controls in collecting tank-IIIT13 by acid and alkali-resistance pneumatic diaphragm pump P14, and Yu Shoushui
Adjustment tank-VT14 in water-level gauge LE10 when " HI-HI ", stop acid and alkali-resistance pneumatic diaphragm pump P14 and P13 action.
2. Wastewater by Electric flocculation oxidation and alkalization
Water-level gauge LE10 is when " HI " in adjustment tank-VT14, and it is pneumatic every pump P15 and the K04 of electric flocculation machine-I to start acid and alkali-resistance,
It is pneumatic every pump P16 and the K05 of electric flocculation machine-II that water-level gauge LE10 starts acid and alkali-resistance when " HI-HI ", side by side, two sets of electric flocculation machines
Stop containing pump operation (K04+P15) and (K05+P16) mode of operation for skyer is low, alternate-running, superelevation is arranged side by side.Now in by water it
Water-level gauge LE11 is when " HI-HI " in the T15 of adjustment tank-VI, and the acid and alkali-resistance of two sets of electric flocculation machines and correspondence is pneumatic synchronously to stop every pump
Only.
Acid and alkali-resistance is pneumatic to be started when pump P17 is in water-level gauge LE11 " HI " in the T15 of adjustment tank-VI, interlocks mixer-II
M02 carries out waste water stirring, now, in the chemicals feeder C02 in alkalization groove T16 with dosing, and is controlled with ph controller PH02
Waste water quality when (can in it is set on ph controller), stops chemicals feeder C02 actions higher than 8.Acid and alkali-resistance pneumatic diaphragm pump P18
By water-level gauge LE12 controls in the T17 of collecting tank-IV, skyer is low stops, and in water-level gauge LE13 in the T18 of adjustment tank-VII by water in
When " HI-HI ", stop acid and alkali-resistance pneumatic diaphragm pump P18 and P17 action.
3. dross dehydration machine is filtered
The dross dehydration machine used in filtering designed by this stage is K02, and the acid and alkali-resistance membrane pump of correspondence is P19, correspondence
The T19 of filtered water collection groove-V, the liquid level in corresponding groove is calculated as " DLE6 " (digital level meter), the filtering completion water of correspondence
Delivery pump is " P20 ".
In setting dross dehydration machine " manual ", " automatic " and " stopping " in control panel, herein different from " filtration system " institute
Its " manual ", " automatic " and " stopping " are set, the behaviour whether dross dehydration machine is " manual ", " automatic " or " stopping " in itself is referred exclusively to herein
Make.
System is when progress is filtered, and lasting aeration to filtration is completed in the T18 of adjustment tank-VII, and filtration pressure is set
Due to 6KG/CM2.(in aeration time-histories, gas piping valve " AV16 " is opened.)
" manual ", " automatic " and " stopping " may be selected in dross dehydration machine K06, and when " manual ", filter pressure is in 6KG/CM2It is lower and
Filtering completes water no longer water outlet and continues more than 5 minutes, represents dross dehydration machine filtering time-histories and has completed, now filtrate is full, stops
Only acid and alkali-resistance pneumatic diaphragm pump P19 action, (dross dehydration machine it) conveyer action, oil hydraulic cylinder release of pressure opens sheet frame, scum silica frost
Filtrate (because of gravity) is unloaded automatically, is transported to hopper by (dross dehydration machine it) conveyer and (is transported to discarded object stockpile manually
Abandoned with to be shipped), oil hydraulic cylinder send pressure, and sheet frame plywood, acid and alkali-resistance pneumatic diaphragm pump P19 actions continue to filter.
During dewaterer " automatic ", " PP02 " gauge pressure continues 6KG/CM2More than (can be adjusted with man-machine setting), corresponding receipts
Collect liquid level gauge DLE6 in the T19 of groove-V, every 10 minutes (can be by man-machine setting) liquid level difference is no more than 1 centimeter, and plate and frame dewaterer is certainly
The dynamic program for completing above-mentioned " manual ".
When dross dehydration machine is set in " stopping ", maintenance shut-downs.
When filtration system carries out " automatic ", start acid and alkali-resistance pneumatic diaphragm pump P19, filtering completes water and enters collecting tank-V
Set liquid level gauge " DLE6 " control acid and alkali-resistance pneumatic diaphragm pump " P20 " " skyer ", water when 50 centimeters of height of water level in T19, groove
Position 10 centimeters " low to stop " of height.
When filtration system carries out " manual ", each equipment and the manually opened test of pipeline valve.
4th, fourth stage-micro-pipe filtering, acid-base neutralization, reverse osmosis filtering and UV oxidations
1. micro-pipe is filtered
The system oozes filtration system for protection is inverse, sets two sets of micro-pipe type filtration systems, and one is high-pressure pump P21+ micro-pipes
The E02 of filter-I；Another is the E03 of high-pressure pump P22+ micro-pipes filter-II；Two sets of systems are by the water-level gauge in the T20 of adjustment tank-VIII
LE14 is controlled, and two system skyer is low to stop, alternate-running, superelevation parallel running.
2. acid-base neutralization
Micro-pipe filtering completes the M03 of mixer-III and acid and alkali-resistance pneumatic diaphragm pump P21 that water enters in neutralization chamber T21, groove
And/or P22 is interlocked, during influent stream, with chemicals feeder C03 actions, it is controlled the pH value in neutralization chamber T21 by ph controller PH03
Stop dosing during less than 7.2 (it can be set in ph controller).The waste water for neutralizing completion enters the T22 of collecting tank-VI, in groove
Water-level gauge LE15 control acid and alkali-resistance pneumatic diaphragm pump P23 skyers it is low stop to the T23 of adjustment tank-Ⅸ to carry out water quality and quantity adjustment it is equal
Homogenize to treat next step.
3. reverse osmosis is filtered
The system releases standard to ensure water-quality COD less than environmental protection and maintains system water outlet water, is divided into two-period form against oozing
Saturating device, first paragraph is inverse to ooze filtration system, sets two sets, one is the E05 of high-pressure pump P24+ reverse osmosis filter-II；It is another to be
The E04 of high-pressure pump P25+ reverse osmosis filter-I；Two sets of systems are controlled by the water-level gauge LE16 in the T23 of adjustment tank-Ⅸ, and two system is high
Beat it is low stop, alternate-running, superelevation parallel running.
70% is only accounted for because reverse osmosis filtering completes water, therefore second segment reverse osmosis filtering (filter efficiency is set：70%+
30%X 70%=70%+21%=91%, system completes efficiency up to ninety percent.), the inverse filtering completion water that oozes of first paragraph enters tune
Water-level gauge LE17 controls are set in the whole T24 of groove-Ⅹ, groove, and high-pressure pump P26 skyers are low stops, and two sections of filterings complete water and enter backwash tank
T18。
4. each stage backwash
Due to backwash process must be carried out after one section of time-histories of filtering, otherwise micro-pipe filter membrane or inverse ooze filter membrane and easily block
And must change, therefore the system design backwashing system, operation tank is backwash tank T25, and operation power is high-pressure pump P27, backwash
Water lines valve (being also backwash sequence) is " V17 ", " V18 ", " V19 ", " V20 " and " V21 ", and backwash time-histories is once in a week (can
It is set by man-machine interface), each backwash is 30 minutes (can set it by man-machine interface), and such as backwash time-histories encounters the system mistake by chance
It is preferential to be filtered into when filtering time-histories, backwash is carried out after the completion of filtering again；Before each backwash stage is carried out, water in anti-wash tank T25
If position meter LE18 is when " LO ", backwash pause in action proceeds backwash action when water-level gauge exceedes " HI ".
The E02 of micro-pipe filter-I and the E03 of micro-pipe filter-II backwash waste are handled again into the T18 of adjustment tank-VII；
The E04 of reverse osmosis filter-I, the E05 of reverse osmosis filter-II and the E06 of reverse osmosis filter-III backwash waste enter adjustment tank-
I T01 is handled again.
5.UV is aoxidized and released
Complete water through reverse osmosis filtering and enter backwash tank T25, after full water in an overflow manner by UV be catalyzed the T26 of groove-I and
UV is catalyzed the T27 of groove-II, into releasing chute T28, and acid and alkali-resistance pneumatic diaphragm pump P28 water-level gauge LE19 controls in releasing chute T28 are high
Beat low stop.Pipeline valve " V22 " is maintained a normally open, and pipeline valve " V23 " keeps normally closed.
5th, aerating system and gas piping valve
The air blower totally three of the system configuration, the A03 of aeration blower-I, the A04 of aeration blower-II and aeration air blast
Machine-IIIA05, every aeration quantity is 10CMM-4000MMAQ.The pipeline of linking and cell body are as described below：
AV01-T01-1, when acid and alkali-resistance pneumatic diaphragm pump P01 starts, gas piping valve is opened.
AV02-T01-2, when acid and alkali-resistance pneumatic diaphragm pump P01 starts, gas piping valve is opened.
AV03-T01-3, when acid and alkali-resistance pneumatic diaphragm pump P01 starts, gas piping valve is opened.
AV04-T01-4, when acid and alkali-resistance pneumatic diaphragm pump P01 starts, gas piping valve is opened.
AV05-T01-5, when acid and alkali-resistance pneumatic diaphragm pump P01 starts, gas piping valve is opened.
AV06-T01-6, when acid and alkali-resistance pneumatic diaphragm pump P01 starts, gas piping valve is opened.
AV07-T01-7, when acid and alkali-resistance pneumatic diaphragm pump P01 starts, gas piping valve is opened.
AV08-T01-8, when acid and alkali-resistance pneumatic diaphragm pump P01 starts, gas piping valve is opened.
AV09-T01-9, when acid and alkali-resistance pneumatic diaphragm pump P01 starts, gas piping valve is opened.
AV10-T01-10, when acid and alkali-resistance pneumatic diaphragm pump P01 starts, gas piping valve is opened.
AV11-T03, when acid and alkali-resistance pneumatic diaphragm pump P03 starts, gas piping valve is opened.
AV12-T04, in the K02 of MVR rapid steamers-I and or-II K03 startup when, gas piping valve open.
AV13-T11, when acid and alkali-resistance pneumatic diaphragm pump P13 starts, gas piping valve is opened.
AV14-T14, when acid and alkali-resistance pneumatic diaphragm pump P14 and/or P15 start, gas piping valve is opened.
AV15-T15, when acid and alkali-resistance pneumatic diaphragm pump P17 starts, gas piping valve is opened.
AV16-T18, when acid and alkali-resistance pneumatic diaphragm pump P19 starts, gas piping valve is opened.
AV17-T20, when high-pressure pump P21 and/or P22 start, gas piping valve is opened.
AV18-T23, when high-pressure pump P24 and/or P25 start, gas piping valve is opened.
AV19-T26, when high-pressure pump P24 and/or P25 and/or P26 starts, gas piping valve is opened.
AV20-T27, when high-pressure pump P24 and/or P25 and/or P26 starts, gas piping valve is opened.
AV21-D04, when medicine is steeped, gas piping valve manual unlocking.If (during bubble medicine when starting at the beginning of system, air blast
Machine not yet starts, and now starts any air blower, and with the manually opened group of air pipe line valve five to ten, be then turned on air
Pipeline valve AV20 is to carry out bubble medicine.)
The technical concepts and features of embodiment of above only to illustrate the invention, its object is to allow be familiar with technique
People understands present disclosure and is carried out, and it is not intended to limit the scope of the present invention, all according to spirit of the invention
The equivalent change or modification that essence is done, should all cover within the scope of the present invention.
Claims (12)
1. cutting fluid recovery and processing system, including four stage processing systems, the four stages processing system are included by pump once
First stage processing system, second stage processing system, phase III processing system and the fourth stage processing system of connection, its
It is characterised by：
The first stage processing system includes passing sequentially through adjustment tank-I, the dross dehydration of the connection of acid and alkali-resistance pneumatic diaphragm pump
Machine-I, collecting tank-I, adjustment tank-II and adjustment tank-III, are provided with oil removing between the adjustment tank-II and the adjustment tank-III
Device；
The second stage processing system includes MVR rapid steamers, circulating slot, oil-water separation tank, collecting tank-II and waste oil and reclaimed
Groove, the MVR rapid steamers pass through water pump formation inner loop, the MVR rapid steamers and the water-oil separating with the circulating slot
Device is connected by pipeline, and the oil-water separation tank is connected with the collecting tank-II by pipeline, the collecting tank-II with it is described
Waste oil accumulator tank is connected by pipeline, between the oil-water separation tank and the collecting tank-II, the collecting tank-II with it is described
Acid and alkali-resistance pneumatic diaphragm pump is set between waste oil accumulator tank；
The phase III processing system includes the adjustment tank-IV being sequentially connected, acidifying groove, collecting tank-III, adjustment tank-V, electricity
Flocculation machine, adjustment tank-VI, alkalization groove, collecting tank-IV, adjustment tank-VII, dross dehydration machine-II and collecting tank-V, the adjustment
Between groove-IV and the acidifying groove, between the collecting tank-III and the adjustment tank-V, the adjustment tank-VI and the alkali
Provided with resistance between change groove, the collecting tank-IV and the adjustment tank-VII, the adjustment tank-VII and the dross dehydration machine-II
Soda acid pneumatic diaphragm pump, working barrel is set between the adjustment tank-V and the electric flocculation machine；
The fourth stage processing system include pass sequentially through high-pressure pump connection adjustment tank-VIII, micro-pipe filter, adjustment tank-
Ⅸth, reverse osmosis filter, adjustment tank-Ⅹ, backwash tank, UV catalysis grooves-I and UV catalysis groove-II, the micro-pipe filter and institute
State and neutralization chamber, collecting tank-VI are set gradually between adjustment tank-Ⅸ, the UV catalysis grooves-II and releasing chute are pneumatic by acid and alkali-resistance
Membrane pump is connected；
The acid and alkali-resistance pneumatic diaphragm pump is connected by five mouthfuls of two valves with air compressor machine.
2. cutting fluid recovery and processing system according to claim 1, it is characterised in that：The MVR rapid steamers steam including MVR
Hair machine-I and MVR rapid steamer-II, the MVR rapid steamers-I and MVR rapid steamers-II are in parallel, and the oil-water separation tank includes profit
Separating tank-I and oil-water separation tank II, the oil-water separation tank-I and oil-water separation tank II are in parallel, the oil-water separation tank-I and
Oil-water separation tank II is connected by pipeline with the adjustment tank-I respectively.
3. cutting fluid recovery and processing system according to claim 1, it is characterised in that：The electric flocculation machine includes electric flocculation
Machine-I and electric flocculation machine-II, the electric flocculation machine-I and electric flocculation machine-II are in parallel.
4. cutting fluid recovery and processing system according to claim 1, it is characterised in that：The micro-pipe filter includes micro-pipe
Filter-I and micro-pipe filter-II, the micro-pipe filter-I and micro-pipe filter-II are in parallel, the micro-pipe filter-I
It is connected respectively with the adjustment tank-VIII with micro-pipe filter-II, micro-pipe filter-I and micro-pipe filter-II difference
It is connected with the backwash tank, the reverse osmosis filter includes reverse osmosis filter-I, reverse osmosis filter-II and reverse osmosis
Filter-III, the reverse osmosis filter-I, reverse osmosis filter-II and reverse osmosis filter-III respectively with the backwash water
Groove is connected by high-pressure pump, the reverse osmosis filter-I, reverse osmosis filter-II and reverse osmosis filter-III respectively with institute
State the connection of adjustment tank-I.
5. cutting fluid recovery and processing system according to claim 1, it is characterised in that：The collecting tank-I, water-oil separating
Groove, collecting tank-II, waste oil accumulator tank and the setting digital level meter of collecting tank-V, the liquid level for monitoring pasta and the water surface,
The adjustment tank-I, adjustment tank-II, adjustment tank-III, adjustment tank-IV, adjustment tank-V, adjustment tank-VI, adjustment tank-VII, adjustment
Groove-VIII, adjustment tank-Ⅸ, adjustment tank-Ⅹ, oil-water separation tank, circulating slot, collecting tank-III, collecting tank-IV, collecting tank-VI and put
Liquid level gauge is set on chute, the acidifying groove, alkalization groove, sets PH to count on neutralization chamber, the acidifying groove, alkalization groove and it is described in
With mixer is set in groove.
6. cutting fluid recovery and processing system according to claim 1, it is characterised in that：The adjustment tank-I, adjustment tank-
IIth, adjustment tank-III, adjustment tank-IV, adjustment tank-V, adjustment tank-VI, adjustment tank-VII, adjustment tank-VIII, adjustment tank-Ⅸ, UV are urged
Change groove-I and UV catalysis grooves-II are connected by gas piping valve with air blower respectively.
7. cutting fluid recovery and processing system according to claim 1, it is characterised in that：The MVR rapid steamers are followed with described
Between annular groove, between the MVR rapid steamers and the oil-water separation tank, between the oil-water separation tank and the collecting tank-II
Motor-driven valve is set, motor-driven valve is set between the backwash tank and the micro-pipe filter, the backwash tank is with described against oozing
Through setting motor-driven valve between filter.
8. cutting fluid recovery and processing system according to claim 1, it is characterised in that：The electric flocculation machine is using tubular type electricity
Flocculation machine.
9. the processing method of cutting fluid recovery and processing system according to claim 1, it is characterised in that：At cutting fluid recovery
The method of reason comprises the following steps：
(1) anti-dandruff oil removing：Metal scraps in waste liquid and oil slick are removed by the way that dross dehydration machine-I and oil expeller are preliminary；
(2) MVR demulsifications and recuperation of heat：During MVR, localized hyperthermia causes organic emulsified base molecular changes property, wherein breast
Chemoattractant molecule hydrophily is destroyed, and is temporarily stored into as water-oil separating material in concentrate, in addition, steam compressed process is because high temperature
So that organic molecule becomes VOC and is partially soluble in vapor, it is liquefied as distillate with vapor and discharges outside MVR, due to
Containing VOC COD pollutants are discharged therewith in water distillation, the long key carbon/benzene of macromolecule being not easily decomposed due to the VOC category of discharge
Ring type organic pollutant, while MVR equipment operations, because compressor operation can discharge substantial amounts of thermal source simultaneously, leads to
Cross running water cooling recovery；
MVR equipment a total of two is entered four and gone out：
Two enter：High-concentration waste water to be processed is needed to enter；Pistonless compressor cooling cycling use of water enters；
Four go out：High pollution condensed water is discharged；Hyperthermal distilled water treats that after-treatment waste water is discharged；Recirculated cooling water is discharged；Low temperature steams
Gas is discharged；
(3) electric flocculation oxidation and the water-oil separating of condensed water：Waste water after MVR is handled enters adjustment tank, is first adjusted with hydrochloric acid
Whole pH value, wastewater electrolytic matter is increased with synchronous, then imports electric flocculation machine with working barrel, now the ring-type carbon key and long key in waste water
Carbon molecules turns into simple small molecule organic pollution because of the oxidability of conductive electric energy, adds and produces hydrogen-oxygen Asia with anode iron
The cladding coagulation of iron makes pollution molecular change big and is able to effectively filtering and removes；
(4) micro-pipe filtering and reverse osmosis filtering
Reverse osmosis processing is added in the most back segment of wastewater treatment, micro-pipe filter is added before reverse osmosis；
(5) UV is aoxidized
Aoxidized in system end plus UV catalysis grooves, ozone free electron base is produced, to remove stink and COD.
10. the processing method of cutting fluid recovery and processing system according to claim 9, it is characterised in that：Institute in step (2)
State above and below being formed after high pollution concentration waste water discharge because of demulsification two layers, upper strata is recyclable oil, lower floor is water and bits slag, is followed
Ring imports in raw wastewater pond and refilters processing.
11. the processing method of cutting fluid recovery and processing system according to claim 9, it is characterised in that：Institute in step (2)
State hyperthermal distilled water to import in adjustment tank after after the discharge of after-treatment waste water, regulating water quality and water treat that next stage is handled.
12. the processing method of cutting fluid recovery and processing system according to claim 9, it is characterised in that：Institute in step (2)
State recirculated cooling water discharge Posterior circle to use, in circulating water chennel, slurry can be supplied as more than design temperature.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201710404278.9A CN107162301A (en) | 2017-06-01 | 2017-06-01 | Cutting fluid recovery and processing system and processing method |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201710404278.9A CN107162301A (en) | 2017-06-01 | 2017-06-01 | Cutting fluid recovery and processing system and processing method |
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| CN107162301A true CN107162301A (en) | 2017-09-15 |
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| CN201710404278.9A Pending CN107162301A (en) | 2017-06-01 | 2017-06-01 | Cutting fluid recovery and processing system and processing method |
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Application publication date: 20170915 |