CN108862856A - A kind of acetate fiber waste water reclaiming processing method - Google Patents
A kind of acetate fiber waste water reclaiming processing method Download PDFInfo
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- CN108862856A CN108862856A CN201810728648.9A CN201810728648A CN108862856A CN 108862856 A CN108862856 A CN 108862856A CN 201810728648 A CN201810728648 A CN 201810728648A CN 108862856 A CN108862856 A CN 108862856A
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- waste water
- acetate fiber
- mgso
- crystallization
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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
- C02F9/00—Multistage treatment of water, waste water or sewage
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- 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
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/14—Purification
- C01D3/16—Purification by precipitation or adsorption
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/40—Magnesium sulfates
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—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
- C02F1/44—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
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- 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
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
Abstract
The invention discloses a kind of acetate fiber waste water reclaiming processing methods, for the high reluctant feature of vinegar fibre waste water salt content, the present invention provides a kind of acetate fiber waste water reclaiming processing method, including process routes such as biochemistry, filtering, ultrafiltration, nanofiltration, evaporation, crystallizations, the zero-emission of final achievable vinegar fibre waste water, Sewage treatment rate is up to 99%.It is low to produce water salt content, can be used as process water and utilize again.The salt rate of recovery is high, and the epsom salt and sodium chloride purity isolated are higher.
Description
Technical field
The present invention relates to technical field of waste water processing, and in particular to a kind of acetate fiber waste water reclaiming processing method, and
Liquid zero emission is realized under lower energy consumption and recycles magnesium sulfate and sodium chloride.
Background technique
In acetate fiber production process, the meeting a large amount of vinegar fibre waste water of output, wastewater through organic matter content height, inorganic salt content
Height, wherein inorganic salts ingredients are mainly magnesium sulfate.Currently, acetate fiber factory to the waste water mainly pass through biochemical oxidation remove it is organic
Sewage treatment plant is emitted into after object.Waste discharge is not able to satisfy environmental emission standard since salt content is higher, and there are secondary pollutions
Risk.Main component is magnesium sulfate in the waste water, and magnesium sulfate may be used as process hides, explosive, papermaking, porcelain, fertilizer in the market
And the industries such as medical treatment, application value with higher.Therefore, such as the magnesium sulfate in this waste water is separated and is utilized again, it can
Generate biggish economic benefit and environmental benefit.
Summary of the invention
The technical problem to be solved by the present invention is to a kind of acetate fiber waste water reclaiming treatment process, by inexpensive, low
Energy consumption, the process of high benefit realize wastewater zero discharge, and isolate the magnesium sulfate and sodium chloride in vinegar fibre waste water.
In order to solve the above-mentioned technical problem, the technical solution adopted by the present invention is:At a kind of acetate fiber waste water reclaiming
Reason method, following steps:
A) acetate fiber waste water is passed through adjusting sedimentation basin, filtrate is passed through biochemical oxidation pond after filtering, by aerobic micro-
Biological decomposition consumes the organic substance in waste water;
B) it is filtered to by biochemical oxidation pond processed waste water;
C) hyperfiltration treatment is carried out again to filtered waste water, for removing macromolecular substances;
D) nanofiltration processing is carried out to the waste liquid after ultrafiltration again, separates sodium salt and magnesium salts;
E) by nanofiltration, treated produces water and carry out reverse osmosis treatment, and obtained concentrate is passed through in sodium chloride crystallization apparatus,
It may separate out sodium chloride crystal salt by thermal method crystallization;Dope after nanofiltration is passed through magnesium sulfate crystallization apparatus, is evaporated, is dense
Contracting, vacuum flashing crystallization, isolate epsom salt.
Further, when crystallizing to sodium chloride solution and Adlerika, discharge part mother liquor to mother liquor crystallization is filled
It sets and carries out crystallization collection carnallite.
Further, the sodium chloride crystallization apparatus includes preheater, degasser, circulating pump, heat exchanger and crystallizer,
The preheater preheats the filtrate after reverse osmosis, and degasser inlet connection preheater is for removing in filtrate
Not condensate steam enters heat exchanger by the filtrate of degassing process after circulating pump, and heat exchanger reconnects crystallizer, crystallizer
Filtrate is flashed, crystallizer is also connected with brine pump and the salt slurry containing crystal salt is pumped into thickener, thickener connection one
A dewaterer.
Further, sodium chloride crystallization apparatus further includes a vapour compression machine, and vapour compression machine will flash in crystallizer
It measures after the both vapor compression heating generated in the process into heat exchanger.
Further, the magnesium sulfate evaporated crystallization device includes MgSO4Preheater, MgSO4Degasser, circulating pump, evaporation
Device, flash tank, vacuum pump and dewaterer, MgSO4Degasser is to by MgSO4MgSO after preheater preheating4Solution is taken off
Gas disposal, the MgSO after degassing process4Solution enters evaporator and is evaporated concentration, and the concentrate after evaporation enters flash tank,
Vacuum pump connects flash tank and carries out vacuum flashing, and the part epsom salt for flashing precipitation enters dewaterer and is separated by solid-liquid separation.
Further, the magnesium sulfate evaporated crystallization device also includes a vapour compression machine, which will dodge
It measures after the both vapor compression heating generated in flash process in steaming pot into evaporator.
From above-mentioned technical proposal it can be seen that the present invention has the following advantages that:Realize liquid zero emission, production water salt content is low,
It can be used as process water to utilize again, the salt rate of recovery is high, and the epsom salt and sodium chloride purity isolated are higher.
Detailed description of the invention
Fig. 1 is process flow diagram of the invention;
Fig. 2 is sodium chloride crystallization apparatus structural schematic diagram in the present invention;
Fig. 3 is magnesium sulfate evaporated crystallization device structural schematic diagram of the present invention.
Specific embodiment
Below according to attached drawing, and with vinegar fibre influent waste water amount it is 500m3/h, water inlet TDS ≈ 7.1g/L, mainly contains sulphur
For sour magnesium ≈ 5.0g/L, sodium chloride ≈ 1.0g/L, organic matter ≈ 1.0g/L and a small amount of carnallite, the present invention is further illustrated
The present invention is handled according to 1 process flow Dichlorodiphenyl Acetate fiber waste water of attached drawing, is passed sequentially through and is adjusted sedimentation basin, oxidation
Pond, filter tank, ultrafiltration and nanofiltration.Nanofiltration produce water enter it is reverse osmosis be concentrated, reverse osmosis produced water can reuse, reverse osmosis concentrated water enter
Sodium chloride crystallization apparatus may separate out sodium chloride crystal salt.Nanofiltration concentrated water, which enters magnesium sulfate evaporated crystallization device, may separate out seven
Water magnesium sulfate crystal salt.Sodium chloride crystallization apparatus and the mother liquor of magnesium sulfate crystallization apparatus output enter carnallite crystallization apparatus, thus
Realize liquid zero emission.
Adjusting sedimentation basin has the function of mixing the cleaning such as filter tank, ultrafiltration waste water in acetate fiber influent waste water and system.
Biochemical oxidation pond can remove most organic matter, and the wastewater through organic matter content for aoxidizing output is lower than 100ppm, be equipped with drum in pond
Blower passes through the organic substance in aerobic microbiological decomposition and consumption waste water.Filter tank can remove the suspended matter in oxidation pond water outlet, drop
The load of low ultrafiltration apparatus.Ultrafiltration apparatus can remove the impurity such as suspended solid, colloid, the COD in water removal, can protect nanofiltration membrane.
Nanofiltration is a kind of pressure-driven membrane separation device between reverse osmosis between ultrafiltration, and nanofiltration membrane aperture is received 3~6
Rice or so, relative to reverse osmosis, nanofiltration still has stronger interception capacity under lower operating pressure, has operation energy consumption phase
To lower advantage;In addition, the special construction of nanofiltration membrane allow certain monovalentions to pass through but retain the multivalence of divalent or more from
Son can achieve certain separating effect.Vinegar fibre waste water can carry out sodium (Na+), magnesium (Mg2+) ion after nanofiltration device
Initial gross separation.Nanofiltration inflow is 500m3/ h, production water side are 450m3/ h, concentrated water side are 50m3/h.Producing water side is that sodium chloride is molten
Liquid, into reverse osmosis unit, the reverse osmosis rate of recovery is 90%, water yield 405m3/ h produces water TDS≤300ppm, can reuse.It is dense
Water is 45m3/ h, NaCl content are about 11g/L, and sodium chloride solution enters can output after sodium chloride crystallizer is evaporated concentration
The sodium chloride crystal salt of about 450kg/h.The main containing magnesium sulfate of nanofiltration concentrated water, sulfuric acid content of magnesium are about 50g/L, are steamed by magnesium sulfate
Sending out crystallization apparatus can be recycled epsom salt about 5.0t/h.Sodium chloride crystallization and magnesium sulfate crystallization are expelled to the carnallite of mother liquor crystallization
Quantum of output is about 100kg/h, and the total water yield of system is 495m3/ h, wastewater recycle rate are greater than 99%.
The sodium chloride crystallization apparatus is as shown in Fig. 2, and implementation steps are as follows:It is pre- that reverse osmosis concentrated water initially enters NaCl
Hot device 1-1 exchanges heat with condensate liquid, and the preliminary concentrated water for obtaining heat enters NaCl degasser 1-2 and carries out stripping, can be by concentrated water
In fixed gas removal NaCl heat exchanger 1-4 is delivered to by NaCl circulating pump 1-9 then from flowing to NaCl crystallizer 1-3,
It is recycled to NaCl crystallizer 1-3, concentrate is dodged in NaCl crystallizer 1-3 after NaCl heat exchanger 1-4 obtains heat
It steams, is concentrated into meeting precipitated sodium chloride crystal salt after a certain concentration, the salt slurry containing crystal salt is delivered to by NaCl brine pump 1-6
NaCl thickener 1-7 carries out initial concentration, then enters back into NaCl dewaterer 1-8 and is dehydrated, and isolates sodium chloride crystallization
Salt.After the steam that concentrated water flashes output in NaCl crystallizer 1-3 carries out compression increasing temperature and pressure by NaCl vapour compression machine 1-5
It can be used as the heat source in NaCl heat exchanger 1-4.For the crystallization purity salt for guaranteeing sodium chloride crystallizer output, discharge unit denominator is needed
Liquid is to the carnallite crystallizer.
The magnesium sulfate evaporated crystallization device is as shown in Fig. 3, and implementation steps are as follows:Nanofiltration concentrated water sequentially enter to
MgSO4Preheater 2-1, MgSO4Degasser 2-2 flow to MgSO by the nanofiltration concentrated water for preheating, deaerating certainly again4Evaporator 2-3 is dense
Water passes through MgSO42-5 evaporative recirculation pump recycles in evaporator, and is concentrated by evaporation, and the secondary steam for evaporating output enters
MgSO4Vapour compression machine 2-4, the steam after increasing temperature and pressure can be used as the heat source of evaporator, discharge after becoming condensed water after heat
It flow to MgSO4Condensation water tank 2-6, passes through MgSO4Condensate pump 2-7 is delivered to MgSO4Preheater 2-1.Concentration after evaporation and concentration
Liquid enters to MgSO4Flash tank 2-9, at this time MgSO4Pass through MgSO in flash tank 2-94Vacuum pump 2-11 carries out decompression and dodges
It steams, part epsom salt can be precipitated in flash distillation, and epsom salt enters dewaterer and is separated by solid-liquid separation, and can be obtained seven water sulfuric acid
Magnesium crystallizes product salt.It is recycled containing solid concentrated water by MgSO42-8 crystallisation cycle pump, and refluxing portion is dodged into evaporator
The steam for steaming output enters MgSO4It is condensed in flash cooler 2-10, makes MgSO4Flash tank 2-9 is maintained at required pressure limit
It is interior.To guarantee MgSO4Purity salt is crystallized, a small amount of mother liquor need to be discharged to carnallite crystallization apparatus in magnesium sulfate evaporated crystallization device.
Carnallite crystallization apparatus need to handle the mother liquor of sodium chloride crystallization apparatus and the discharge of magnesium sulfate crystallization apparatus, the mother liquor of discharge
It measures less, salt content height, spray dryer can be directlyed adopt or vibrating screen is dried, to realize the liquid zero-emission of whole system
It puts.
Claims (6)
1. a kind of acetate fiber waste water reclaiming processing method, it is characterised in that include the following steps:
A) acetate fiber waste water is passed through adjusting sedimentation basin, filtrate is passed through biochemical oxidation pond after filtering, passes through aerobic microbiological
Organic substance in decomposition and consumption waste water;
B) it is filtered to by biochemical oxidation pond processed waste water;
C) hyperfiltration treatment is carried out again to filtered waste water, for removing macromolecular substances;
D) nanofiltration processing is carried out to the waste liquid after ultrafiltration again, separates sodium salt and magnesium salts;
E) by nanofiltration, treated produces water and carry out reverse osmosis treatment, and obtained concentrate is passed through in sodium chloride crystallization apparatus, passes through
Thermal method crystallization may separate out sodium chloride crystal salt;Dope after nanofiltration is passed through magnesium sulfate crystallization apparatus, be evaporated, be concentrated,
Vacuum flashing crystallization, isolates epsom salt.
2. according to right want 1 described in acetate fiber waste water reclaiming processing method, it is characterised in that:To sodium chloride solution and
Discharge part mother liquor to mother liquor crystallization device carries out crystallization and collects carnallite when Adlerika is crystallized.
3. according to right want 1 described in acetate fiber waste water reclaiming processing method, it is characterised in that:The sodium chloride crystallization dress
It sets including NaCl preheater, NaCl degasser, NaCl circulating pump, NaCl heat exchanger and NaCl crystallizer, NaCl preheater pair
Filtrate after reverse osmosis is preheated, and NaCl degasser inlet connection NaCl preheater is for removing not coagulating in filtrate
Water vapour enters NaCl heat exchanger by the filtrate of degassing process after NaCl circulating pump, and NaCl heat exchanger reconnects NaCl
Crystallizer, NaCl crystallizer flash filtrate, and NaCl crystallizer is also connected with brine pump and is pumped into the salt slurry containing crystal salt
Increase in the thick device of NaCl, NaCl thickener connects a dewaterer.
4. acetate fiber waste water reclaiming processing method according to claim 3, it is characterised in that:Sodium chloride crystallization apparatus is also
Including a vapour compression machine, vapour compression machine is measured after the both vapor compression generated in flash process in crystallizer heats up into heat exchange
Device.
5. acetate fiber waste water reclaiming processing method according to claim 3, it is characterised in that:The magnesium sulfate evaporation
Crystallization apparatus includes MgSO4Preheater, MgSO4Degasser, circulating pump, evaporator, flash tank, vacuum pump and dewaterer,
MgSO4Degasser is to by MgSO4MgSO after preheater preheating4Solution is de-gassed, the MgSO after degassing process4It is molten
Liquid enters evaporator and is evaporated concentration, and the concentrate after evaporation enters flash tank, and vacuum pump connection flash tank carries out decompression sudden strain of a muscle
It steams, the part epsom salt for flashing precipitation enters dewaterer and is separated by solid-liquid separation.
6. acetate fiber waste water reclaiming processing method according to claim 5, it is characterised in that:The magnesium sulfate evaporation
Crystallization apparatus also includes a vapour compression machine, the both vapor compression liter which will generate in flash process in flash tank
Wen Houliang enters evaporator.
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CN110204136A (en) * | 2019-04-07 | 2019-09-06 | 李英劼 | The method that electroplating waste water resource utilizes |
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Application publication date: 20181123 |