CN108862856A - A kind of acetate fiber waste water reclaiming processing method - Google Patents

A kind of acetate fiber waste water reclaiming processing method Download PDF

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Publication number
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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China
Prior art keywords
nacl
waste water
crystallization
acetate fiber
mgso
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CN201810728648.9A
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Chinese (zh)
Inventor
夏清
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Shanghai Wen Jie Environmental Engineering Office
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Shanghai Wen Jie Environmental Engineering Office
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Priority to CN201810728648.9A priority Critical patent/CN108862856A/en
Publication of CN108862856A publication Critical patent/CN108862856A/en
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    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00Multistage treatment of water, waste water, or sewage
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01DCOMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00Halides of sodium, potassium or alkali metals in general
    • C01D3/04Chlorides
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01DCOMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00Halides of sodium, potassium or alkali metals in general
    • C01D3/14Purification
    • C01D3/16Purification by precipitation or adsorption
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01FCOMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F5/00Compounds of magnesium
    • C01F5/40Magnesium sulfates
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/001Processes for the treatment of water whereby the filtration technique is of importance
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/02Treatment of water, waste water, or sewage by heating
    • C02F1/04Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/02Treatment of water, waste water, or sewage by heating
    • C02F1/04Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/041Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/44Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/44Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/442Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/44Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F2001/007Processes including a sedimentation step
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/34Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
    • C02F2103/36Nature 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
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00Biological treatment of water, waste water, or sewage
    • C02F3/02Aerobic 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

A kind of acetate fiber waste water reclaiming processing method
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.
CN201810728648.9A 2018-07-05 2018-07-05 A kind of acetate fiber waste water reclaiming processing method Pending CN108862856A (en)

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004013048A2 (en) * 2002-08-02 2004-02-12 University Of South Carolina Production of purified water and high value chemicals from salt water
CN105540967A (en) * 2015-12-09 2016-05-04 大唐国际化工技术研究院有限公司 Processing method for reducing and recycling organic waste water and processing system
CN106396274A (en) * 2016-11-07 2017-02-15 四川普什醋酸纤维素有限责任公司 Treatment process of cellulose acetate wastewater
CN107324612A (en) * 2017-08-29 2017-11-07 南通醋酸纤维有限公司 Acetate fiber produces waste water reclaiming recovery method and its recovery system
CN107352727A (en) * 2017-09-07 2017-11-17 北京中洁蓝环保科技有限公司 A kind of coal chemical industrial waste water goes out salt Zero discharging system and its implementation
CN107758962A (en) * 2017-11-07 2018-03-06 博天环境工程(北京)有限公司 A kind of system of the preparing magnesium sulfate from desulfurization wastewater

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2004013048A2 (en) * 2002-08-02 2004-02-12 University Of South Carolina Production of purified water and high value chemicals from salt water
CN105540967A (en) * 2015-12-09 2016-05-04 大唐国际化工技术研究院有限公司 Processing method for reducing and recycling organic waste water and processing system
CN106396274A (en) * 2016-11-07 2017-02-15 四川普什醋酸纤维素有限责任公司 Treatment process of cellulose acetate wastewater
CN107324612A (en) * 2017-08-29 2017-11-07 南通醋酸纤维有限公司 Acetate fiber produces waste water reclaiming recovery method and its recovery system
CN107352727A (en) * 2017-09-07 2017-11-17 北京中洁蓝环保科技有限公司 A kind of coal chemical industrial waste water goes out salt Zero discharging system and its implementation
CN107758962A (en) * 2017-11-07 2018-03-06 博天环境工程(北京)有限公司 A kind of system of the preparing magnesium sulfate from desulfurization wastewater

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