CN105502782A - Technology for recovering water resources and salt from coking wastewater in coal chemical industry - Google Patents

Technology for recovering water resources and salt from coking wastewater in coal chemical industry Download PDF

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CN105502782A
CN105502782A CN201510881304.8A CN201510881304A CN105502782A CN 105502782 A CN105502782 A CN 105502782A CN 201510881304 A CN201510881304 A CN 201510881304A CN 105502782 A CN105502782 A CN 105502782A
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water
nanofiltration
salt
waste water
strong brine
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CN105502782B (en
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肖国军
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HUNAN XIANGNIU ENVIRONMENT PROTECTING INDUSTRY Co Ltd
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HUNAN XIANGNIU ENVIRONMENT PROTECTING INDUSTRY Co Ltd
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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
    • 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
    • C01D3/06—Preparation by working up brines; seawater or spent lyes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
    • 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
    • C02F1/24—Treatment of water, waste water, or sewage by flotation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/722—Oxidation by peroxides
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/12—Halogens or halogen-containing compounds
    • C02F2101/14—Fluorine or fluorine-containing compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
    • C02F5/02—Softening water by precipitation of the hardness
    • C02F5/06—Softening water by precipitation of the hardness using calcium compounds

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Removal Of Specific Substances (AREA)

Abstract

A technology for recovering water resources and salt from coking wastewater in the coal chemical industry comprises the following steps: the wastewater is subjected to defluorination chemical treatment and subjected to sodium carbonate softening and precipitating treatment simultaneously, an advanced oxidation process is used for TOC (total organic carbon) degradation, a multi-medium and activated carbon filter is used for filtering separation, ultrafiltration is performed, nanofiltration membrane separation is performed, calcium and magnesium ions are separated, the calcium and magnesium ions in water produced through nanofiltration are lower than 2 mg/L, CaF2 crystallization scaling is hard to form, and nanofiltration passing liquid and nanofiltration strong brine are obtained; the nanofiltration passing liquid and the nanofiltration strong brine are treated respectively. Fluoride ions, hardness and organic carbon in the wastewater are removed, separation of multivalent salt and monovalent salt as well as concentration and evaporative crystallization of the salt is realized, more than 98% of the water resources is recovered, more than 95% of the salt resources are recovered, secondary hazardous waste is not produced, the system operation cost is reduced, and the problem about resource recovery and the environmental problem are solved finally.

Description

A kind of Coal Chemical Industry coking chemical waste water water resources and salt recovery process
Technical field
The present invention relates to field of environment engineering technology, be specially a kind of Coal Chemical Industry coking chemical waste water water resources and salt recovery process.
Background technology
Environmental Protection Department issue on April 21st, 2014 " about in the notice dissolving strengthening ring keeping reason in the serious superfluous contradiction process of production capacity " explicitly calls for " coking chemical waste water adopts pre-treatment (gravity oil-removing method, coagulant sedimentation, oil removal by air bubbling method)+nitrated, denitrification biochemical processing; the rear wastewater containing phenol and cyanide reuse of process, must not arrange outward ".The zero release of Coal Chemical Industry coking chemical waste water bio-chemical effluent is very difficult, it is world-class technical barrier, Major Difficulties is that in coking chemical waste water bio-chemical effluent, TOC content is higher, saltiness is high, hardness is higher, fluoridize object height, this type of waste component is complicated, must capture several technical barrier and just can accomplish real zero release and resource reclaim.Domestic typical case adopts technique to make a living and dissolves hydromining lime soften for sewage+filtration+membrane concentration+evaporation, finishing operation evaporation kettle base solution is due to containing TOC, calcium, magnesium, fluorion and a large amount of sulfate ion, evaporation kettle base solution cannot crystallization, formed and adhere to strong brine slurries, finally can only do the useless process of danger.The rate of recovery of water is at about 92%-95%, and salt cannot reclaim.Therefore, current domestic prevailing technology does not accomplish zero release and the resource reclaim of complete meaning.
Summary of the invention
Technical problem solved by the invention is to provide a kind of Coal Chemical Industry coking chemical waste water water resources and salt recovery process, thus solves the problem in above-mentioned background technology.
Technical problem solved by the invention realizes by the following technical solutions:
A kind of Coal Chemical Industry coking chemical waste water water resources and salt recovery process, comprise the steps:
(1) to FLUORIDE REMOVAL IN WASTEWATER chemical treatment, fluorion is reduced to below 0.5mg/L;
(2) sodium carbonate is carried out to the waste water of step (1) simultaneously soften precipitation process, total hardness is reduced to below 150mg/L;
(3) advanced oxidation processes is adopted to carry out TOC degraded to the waste water that step (2) obtains;
(4) in the waste water processed step (3), suspended substance carries out multimedium and activated charcoal filter filtering separation, suspended substance particle diameter is greater than 5um material and retains;
(5) waste water obtained step (4) adopts ultrafiltration to retain, and is greater than 0.05um material retains particle diameter;
(6) carry out nanofiltration membrane separation to the waste water that step (5) obtains, be separated by calcium ions and magnesium ions, nanofiltration produces water calcium ions and magnesium ions lower than below 2mg/L, is difficult to form CaF 2crystallization fouling, obtains nanofiltration by liquid and nanofiltration strong brine;
(7) by liquid, the separation of reverse osmosis salt solution is carried out to the nanofiltration of step (6), waste water water resources reclaims more than 70%, the monovalent salt strong brine obtained carries out reverse osmosis concentration, monovalent salt is concentrated, sodium-chlor is concentrated to 12000 ~ more than 15000mg/L, and the strong brine obtained enters to adopt ED electrodialysis to concentrate, and sodium-chlor is concentrated to 120000 ~ 150000mg/L, the strong brine obtained carries out evaporative crystallization, obtains crystallization sodium chloride salt;
(8) the nanofiltration strong brine obtained step (6) carries out fluorinated process, fluorion is reduced to below 0.5mg/L, and carry out sodium carbonate and soften precipitation process, total hardness is reduced to below 80mg/L, again suspended substance in water is carried out multimedium and activated charcoal filter filtering separation, and carry out fluorinated process to strong brine, water outlet fluorion is less than 0.5mg/L, then adopt ultrafiltration to retain, colloid, microorganism, fine particulate matter are retained; The ultrafiltrate obtained adopts resin absorption organism, remove strong brine TOC, and adopt resin to soften, remove strong brine hardness, finally carry out nanofiltration membrane separation, further sodium sulfate is separated with sodium-chlor and concentrated vitriol sodium, after concentrated, sodium sulfate concentration is 10000 ~ 15000mg/L, nanofiltration permeate enters step (7), and adopt ED electrodialysis to concentrate to nanofiltration strong brine, sodium sulfate is concentrated to 120000 ~ 150000mg/L, and evaporative crystallization is carried out to strong brine, obtain crystallization five aqueous sodium persulfate salt.
In the present invention, as the preferred technical scheme of one, fluorinated process adopts calcium chloride, lime chemical technology is carried out, and adopted aluminium sesquioxide as adsorption medium, makes fluorion go out water-content and is less than 0.5mg/L.
In the present invention, as the preferred technical scheme of one, FLUORIDE REMOVAL IN WASTEWATER chemical treatment, sodium carbonate are softened precipitation process and are comprised the steps:
First, feeding lime and calcium chloride in first order reaction pond, utilize Ca wherein 2++ OH -with the F in waste water -+ Mg 2+reaction generates CaF2+Mg (OH) 2 flocs unit, and the fluorion removed in water body has gone out magnesium ion simultaneously, utilizes coagulative precipitation device or air-floating apparatus, is separated by solid-liquid, reduce hardness concentration;
Then, the water outlet of first order reaction pond enters fluorion device, is separated by Calcium Fluoride (Fluorspan) with magnesium hydrate precipitate, and reduce fluorion and magnesium hardness concentration, water outlet enters in second order reaction pond, and second order reaction adds sodium carbonate in pond, utilizes CO3 wherein 2-with the Ca in waste water 2+reaction generates CaCO3 flocs unit, removes the calcium ion in water body; Utilize coagulative precipitation device or air-floating apparatus, solid-liquid is separated, reduce hardness concentration;
Finally, the water outlet of second order reaction pond enters in coagulative precipitation tank, carries out mud-water separation;
In first order reaction pond and second order reaction pond, add coagulating agent, described coagulating agent is the aqueous solution of chloride containing aluminium 10wt%, anionic polyacrylamide 0.1wt% simultaneously.
In the present invention, in step (3), advanced oxidation processes adopts ozone+hydrogen peroxide, and ozone dosage is 50mg/L, and hydrogen peroxide dosage is 30mg/L, and TOC degrades by these two kinds of oxygenants, and TOC is reduced to below 50mg/L.
In the present invention, step (7) and step (8) all utilize MVR vaporizer to carry out evaporative crystallization process.
In the present invention, sodium carbonate softens precipitation process and comprises following aspect:
First, feeding lime and calcium chloride in reaction tank in step (1), utilizes Ca wherein 2++ OH -with the F in waste water -+ Mg 2+reaction generates CaF2+Mg (OH) 2 flocs unit, and the fluorion removed in water body has gone out magnesium ion simultaneously; Reaction tank water outlet enters coagulative precipitation device or air-floating apparatus, is separated by solid-liquid, reduces hardness concentration;
Its two, reaction tank adds sodium carbonate in the step (2), utilizes CO3 wherein 2-with the Ca in waste water 2+reaction generates CaCO3 flocs unit, removes the calcium ion in water body; Reaction tank water outlet enters coagulative precipitation device or air-floating apparatus, is separated by solid-liquid, reduces hardness concentration;
Its three, adopt nanofiltration calcium ions and magnesium ions to be carried out separations in the step (6) concentrated;
Its four, is adopted in the nanofiltration strong brine that step (6) is obtained and adds sodium carbonate, utilize CO3 wherein 2-with the Ca in waste water 2+reaction generates CaCO3 precipitation, removes the calcium ion in water body; Reaction tank water outlet enters coagulative precipitation device, solid-liquid separation, reduces hardness concentration;
Its five, in step (8), adopt soften resin strong brine hardness is removed.
In the present invention, TOC removes and have employed following aspect:
One, in step (3), advanced oxidation processes adopts ozone+hydrogen peroxide, and ozone dosage is 50mg/L, and hydrogen peroxide dosage is 30mg/L, and TOC degrades by these two kinds of oxygenants, and TOC is reduced to below 50mg/L;
Its two, adopt charcoal absorption TOC in the step (4), TOC be reduced to below 30mg/L;
Its three, TOC carries out being separated and concentrate by nanofiltration in the step (6), and TOC is concentrated 4 times, and the dense water TOC of nanofiltration is at about 120mg/L;
Its four, nanofiltration strong brine adopts charcoal absorption TOC in the step (8), and TOC is reduced to below 80mg/L;
Its five, the ultrafiltrate that obtains in step (8) adopts resin absorption organism, and TOC is reduced to below 10mg/L.
In the present invention, monovalent salt and a polyvalent salt carry out being separated employing step (6) nanofiltration technique, and in nanofiltration strong brine, sodium sulphate content is greater than 80%, and sodium chloride content is less than 20%; Nanofiltration is less than 5% by sodium sulphate content in liquid, and sodium chloride content is greater than 95%.
In the present invention, sodium sulfate salt purifying adopts step (8), and strong brine total hardness reduced respectively, content is less than 1mg/L, and content of fluoride ion is less than 1mg/L; TOC content is less than 10mg/L.
In the present invention, the crystallization of sodium chloride salt concentration and evaporation adopts step (7), sodium-chlor strong brine TDS is brought up to 8000 ~ 10000mg/L from 2500 ~ 4000mg/L, sodium-chlor strong brine is brought up to 12000 ~ 15000mg/L, sodium chloride concentration is brought up to 100000 ~ 150000mg/L, sodium-chlor strong brine is carried out evaporative crystallization, obtains 95% sodium-chlor.
In the present invention, the crystallization of sodium sulfate salt concentration and evaporation adopts step (8), strong brine TDS is brought up to 8000 ~ 10000mg/L from 3000 ~ 4000mg/L, strong brine TDS is brought up to 120000 ~ 150000mg/L, sodium sulfate strong brine is carried out evaporative crystallization, obtains five aqueous sodium persulfates of about 94% purity.
Owing to have employed above technical scheme, the present invention has following beneficial effect:
Present invention process adopts isolation and purification technique, fluorinion in waste water, hardness, organic carbon are removed, by the concentrated and evaporative crystallization of being separated of a polyvalent salt and monovalent salt, salt, recycle-water resource more than 98% (micro-moisture is taken away with solidification sludge), reclaim the salt resource of more than 95%, do not produce secondary danger useless, reduce system operation cost, final solution resource reclaim and environmental problem.
Reclaim 92 ~ 95% relative to domestic main flow technique of zero discharge waste water water resources, salt cannot reclaim, a small amount of solid waste garbage loading embeading, and have the useless disposal of a large amount of danger, the present invention exists significant beneficial effect and outstanding inventive features.
Embodiment
The technique means realized to make the present invention, creation characteristic, reaching object and effect is easy to understand, below in conjunction with specific embodiment, setting forth the present invention further.
Embodiment
A kind of Coal Chemical Industry coking chemical waste water water resources and salt recovery process, comprise the steps:
(1) to FLUORIDE REMOVAL IN WASTEWATER chemical treatment, fluorion is reduced to below 0.5mg/L;
(2) sodium carbonate is carried out to the waste water of step (1) simultaneously soften precipitation process, total hardness is reduced to below 150mg/L;
(3) advanced oxidation processes is adopted to carry out TOC degraded to the waste water that step (2) obtains, advanced oxidation processes adopts ozone+hydrogen peroxide, ozone dosage is 50mg/L, hydrogen peroxide dosage is 30mg/L, TOC degrades by these two kinds of oxygenants, TOC is reduced to below 50mg/L, because in coking chemical waste water bio-chemical effluent, pollutant kind is various, complicated component, containing macromolecular compound and nitrogenous, oxygen, the heterocyclic organic compounds of sulphur difficult degradation, softening settling tank water outlet contains the materials such as the zoogloea Extracellular enzyme of trace, be easy to produce organic dirt to reclaiming system organic membrane block up, organic dirt must be reduced and block up the factor.The waste water organic contamination factor is through biochemical degradation, the pollution factor being difficult to biochemical degradation can only pass through chemical degradation, and the prerequisite of pollution factor material generation chemical reaction is that pollution substance molecule must must possess enough large energy with chemical molecule generation effective collision and reactant molecule.Molecule activation decomposition apparatus is by the more polyoxygenated molecule of dissolved under pressure, effectively the electrostatic repulsion forces of the molecule valence electron cloud of collision is mutually reduced, thus the repulsive force overcome between valence electron cloud, the formation of the fracture of original chemical bond and new chemical bond is made to serve powerful outer energy, more molecule becomes activated molecule, add the percentage ratio of activated molecule, thus effective collision number of times in the unit time is significantly increased, the probability of molecular impact can be improved, increase the collision energy of molecule, extend the collision time of reaction molecular, thus quickening chemical reaction velocity,
(4) in the waste water processed step (3), suspended substance carries out multimedium and activated charcoal filter filtering separation, suspended substance particle diameter is greater than 5um material and retains;
(5) waste water obtained step (4) adopts ultrafiltration to retain, and is greater than 0.05um material retains particle diameter;
(6) carry out nanofiltration membrane separation to the waste water that step (5) obtains, be separated by calcium ions and magnesium ions, nanofiltration produces water calcium ions and magnesium ions lower than below 2mg/L, is difficult to form CaF2 crystallization fouling, obtains nanofiltration by liquid and nanofiltration strong brine;
(7) by liquid, the separation of reverse osmosis salt solution is carried out to the nanofiltration of step (6), waste water water resources reclaims more than 70%, the monovalent salt strong brine obtained carries out reverse osmosis concentration, monovalent salt is concentrated, sodium-chlor is concentrated to 12000 ~ more than 15000mg/L, and the strong brine obtained enters to adopt ED electrodialysis to concentrate, and sodium-chlor is concentrated to 120000 ~ 150000mg/L, the strong brine obtained carries out evaporative crystallization, obtains crystallization sodium chloride salt;
(8) the nanofiltration strong brine obtained step (6) carries out fluorinated process, fluorion is reduced to below 0.5mg/L, and carry out sodium carbonate and soften precipitation process, total hardness is reduced to below 80mg/L, again suspended substance in water is carried out multimedium and activated charcoal filter filtering separation, and carry out fluorinated process to strong brine, water outlet fluorion is less than 0.5mg/L, then adopt ultrafiltration to retain, colloid, microorganism, fine particulate matter are retained; The ultrafiltrate obtained adopts resin absorption organism, remove strong brine TOC, and adopt resin to soften, remove strong brine hardness, finally carry out nanofiltration membrane separation, further sodium sulfate is separated with sodium-chlor and concentrated vitriol sodium, after concentrated, sodium sulfate concentration is 10000 ~ 15000mg/L, nanofiltration permeate enters step (7), and adopt ED electrodialysis to concentrate to nanofiltration strong brine, sodium sulfate is concentrated to 120000 ~ 150000mg/L, and evaporative crystallization is carried out to strong brine, obtain crystallization five aqueous sodium persulfate salt.
The fluorinated process of above-mentioned step (1) and step (8) adopts calcium chloride, lime chemical technology is carried out, and adopted aluminium sesquioxide as adsorption medium, makes fluorion go out water-content and is less than 0.5mg/L.
FLUORIDE REMOVAL IN WASTEWATER chemical treatment, sodium carbonate are softened precipitation process and are comprised the steps:
First, feeding lime and calcium chloride in first order reaction pond, utilize Ca wherein 2++ OH -with the F in waste water -+ Mg 2+reaction generates CaF2+Mg (OH) 2 flocs unit, and the fluorion removed in water body has gone out magnesium ion simultaneously, utilizes coagulative precipitation device or air-floating apparatus, is separated by solid-liquid, reduce hardness concentration,
Its chemical equation is as follows:
Mg 2++2OH -→Mg(OH) 2↓
2F -+Ca 2+→CaF 2↓
Ca 2++SO4 2-=CaSO 4↓；
Then, the water outlet of first order reaction pond enters fluorion device, is separated by Calcium Fluoride (Fluorspan) with magnesium hydrate precipitate, and reduce fluorion and magnesium hardness concentration, water outlet enters in second order reaction pond, and second order reaction adds sodium carbonate in pond, utilizes CO3 wherein 2-with the Ca in waste water 2+reaction generates CaCO3 flocs unit, removes the calcium ion in water body; Utilize coagulative precipitation device or air-floating apparatus, be separated by solid-liquid, reduce hardness concentration, its chemical equation is as follows:
CaSO 4+Na 2CO 3→CaCO 3↓+Na 2SO 4
CaCl 2+Na 2CO 3→CaCO 3↓+2NaCl
MgSO 4+Na 2CO 3→MgCO 3↓+Na 2SO 4；
Finally, the water outlet of second order reaction pond enters in coagulative precipitation tank, carries out mud-water separation;
In first order reaction pond and second order reaction pond, add coagulating agent, described coagulating agent is the aqueous solution of chloride containing aluminium 10wt%, anionic polyacrylamide 0.1wt%, after calcium chloride sofening treatment, can generate CaCO in water simultaneously 3, CaF 2with Mg (OH) 2etc. the material being insoluble in water, be precipitated out from water.These throw outs usually can not form macrobead thing, and some then suspends in water in colloidal state.When Organic substance in water exists, organism particulate then can be adsorbed on these colloidal solids, is formed " electrostatic double layer ", thus makes throw out colloid can not aggregate into macrobead thing to precipitate.Therefore, calcium chloride sofening treatment and coagulating treatment are carried out simultaneously, and coagulating agent can remove some organism harmful to precipitation process from water, is conducive to sedimentary precipitation.Simultaneously the solidifying wadding that formed of coagulating treatment also can the colloid coprecipitation that formed of adsorbing chlorinated calcium.
Consider that in the dense water of NF or the dense water of RO, water ratio is also higher, directly carry out evaporation can energy consumption higher.For reducing the evaporation process water yield, in step (7) and step (8), evaporation unit front end adopts ED electrodialysis process to carry out reconcentration to dense water, reduces the evaporation process water yield.Electroosmose process (electrodialysis(ED)) be the effect utilizing ion-exchange membrane and electric field, by force ion is attracted to electrode place, cause the ionic concn of electrode middle part greatly to decline, thus a kind of method of obtained fresh water.Generally water intermediate ion freely can pass through ion-exchange membrane.Ion-exchange membrane is a kind of functional membrane, is divided into anion-exchange membrane and cationic exchange membrane, (being called for short cavity block and anode membrane).Anode membrane only allows positively charged ion only to allow negatively charged ion to pass through by cavity block, the selective penetrated property of Here it is ion-exchange membrane.Extra electric field effect under, the moon in the aqueous solution, positively charged ion can respectively to anode and movable cathode, if a kind of exchange membrane is added in centre, just may reach and be separated concentrated object.
In the present invention, step (7) and step (8) all utilize MVR vaporizer to carry out evaporative crystallization process.Wherein, MVR vaporizer is utilized to carry out evaporative crystallization process.Waste water will the dense water of generating portion after nanofiltration and reverse osmosis membrane processing, concentrates most of organism in original waste water and salt and grade pollutent in dense water.Because " about in the notice dissolving strengthening ring keeping reason in the serious superfluous contradiction process of production capacity " (No. (2014) 55, environment-development) requires that coking chemical waste water must not be arranged outward, if the salinity in dense water circulates in systems in which always, salinity will constantly be accumulated, reverse osmosis system water-yielding capacity can be caused to decline and even to cause structure deteriorate, therefore must carry out suitable process to dense water.The present invention adopts the mode of evaporation to process dense water.MVR vaporizer utilizes compressor that the secondary steam that vaporizer produces is carried out compression and its pressure and temperature is raised, then makes vaporizer thermal source and substitute fresh steam.Realize the recycling of heat energy in secondary steam, make the heat energy recycling of vaporizer.As long as provide a small amount of power driven compressor work not need fresh steam just can make vaporizer heat energy recycling, consecutive evaporation.In thermodynamics, MVR vaporizer also can be understood as open type heat pump.The effect of compressor is not the heat producing evaporation needs, but the heat of conveying vaporizer forms recycle heat.MVR vaporizer is vaporizer technology of new generation, is a kind of new and high technology of energy-conserving and environment-protective.MVR vaporizer unit power consumption amount is different according to material characteristic, general often evaporation one ton of water consumption 25-70 degree electricity, and Conventional vaporizer consumes 1.25 tons of fresh steam, the fresh steam of 3 single-effect evaporator consumption about 0.4 ton, to same solution, MVR energy-output ratio and production cost, significantly lower than Conventional vaporizer, are a kind of high-new energy-conservation evaporation techniques.MVR vaporizer does not need recirculated cooling water, does not have cooling-water consumption.Do not need to build the coal firing boiler of high pollution or the oil-firing boiler of high cost.MVR vaporizer more to be economized on water more environmental protection than Conventional vaporizer.MVR evaporator application scope is wide, and the field of all Conventional vaporizer application is all applicable to MVR vaporizer, and MVR evaporator evaporation temperature is low, have a narrow range of temperature, evaporate gentleness is more suitable for thermosensitive solution.Solution flow process in vaporizer is short, and the residence time, short solute should not go bad.MVR vaporizer adopts full-automatic computer to control, and system performance is more stable.Also can run continuously at low load.MVR vaporizer is the State Scientific and Technological Commission of National Development and Reform Committee power-saving technology promotion project, and meet national energy-saving and reduce discharging and environmental protection new and high technology promoted extension, there is special fund support in government.MVR vaporizer construction cost is than Conventional vaporizer height about 2-3 times, but due to save energy, running cost is low, and the general energy-conservation expense running 2 years can offset construction investment in early stage.
More than show and describe ultimate principle of the present invention and principal character and advantage of the present invention.The technician of the industry should understand; the present invention is not restricted to the described embodiments; what describe in above-described embodiment and specification sheets just illustrates principle of the present invention; without departing from the spirit and scope of the present invention; the present invention also has various changes and modifications, and these changes and improvements all fall in the claimed scope of the invention.Application claims protection domain is defined by appending claims and equivalent thereof.

Claims (5)

1. Coal Chemical Industry coking chemical waste water water resources and a salt recovery process, is characterized in that: comprise the steps:
(1) to FLUORIDE REMOVAL IN WASTEWATER chemical treatment, fluorion is reduced to below 0.5mg/L;
(2) sodium carbonate is carried out to the waste water of step (1) simultaneously soften precipitation process, total hardness is reduced to below 150mg/L;
(3) advanced oxidation processes is adopted to carry out TOC degraded to the waste water that step (2) obtains;
(4) in the waste water processed step (3), suspended substance carries out multimedium and activated charcoal filter filtering separation, suspended substance particle diameter is greater than 5um material and retains;
(5) waste water obtained step (4) adopts ultrafiltration to retain, and is greater than 0.05um material retains particle diameter;
(6) carry out nanofiltration membrane separation to the waste water that step (5) obtains, be separated by calcium ions and magnesium ions, nanofiltration produces water calcium ions and magnesium ions lower than below 2mg/L, is difficult to form CaF2 crystallization fouling, obtains nanofiltration by liquid and nanofiltration strong brine;
(7) by liquid, the separation of reverse osmosis salt solution is carried out to the nanofiltration of step (6), waste water water resources reclaims more than 70%, the monovalent salt strong brine obtained carries out reverse osmosis concentration, monovalent salt is concentrated, sodium-chlor is concentrated to 12000 ~ more than 15000mg/L, and the strong brine obtained enters to adopt ED electrodialysis to concentrate, and sodium-chlor is concentrated to 120000 ~ 150000mg/L, the strong brine obtained carries out evaporative crystallization, obtains crystallization sodium chloride salt;
(8) the nanofiltration strong brine obtained step (6) carries out fluorinated process, fluorion is reduced to below 0.5mg/L, and carry out sodium carbonate and soften precipitation process, total hardness is reduced to below 80mg/L, again suspended substance in water is carried out multimedium and activated charcoal filter filtering separation, and carry out fluorinated process to strong brine, water outlet fluorion is less than 0.5mg/L, then adopt ultrafiltration to retain, colloid, microorganism, fine particulate matter are retained; The ultrafiltrate obtained adopts resin absorption organism, remove strong brine TOC, and adopt resin to soften, remove strong brine hardness, finally carry out nanofiltration membrane separation, further sodium sulfate is separated with sodium-chlor and concentrated vitriol sodium, after concentrated, sodium sulfate concentration is 10000 ~ 15000mg/L, nanofiltration permeate enters step (7), and adopt ED electrodialysis to concentrate to nanofiltration strong brine, sodium sulfate is concentrated to 120000 ~ 150000mg/L, and evaporative crystallization is carried out to strong brine, obtain crystallization five aqueous sodium persulfate salt.
2. a kind of Coal Chemical Industry coking chemical waste water water resources as claimed in claim 1 and salt recovery process, it is characterized in that: in step (1) and step (8), fluorinated process adopts calcium chloride, lime chemical technology is carried out, and adopt aluminium sesquioxide as adsorption medium, make fluorion go out water-content and be less than 0.5mg/L.
3. a kind of Coal Chemical Industry coking chemical waste water water resources as claimed in claim 2 and salt recovery process, is characterized in that: FLUORIDE REMOVAL IN WASTEWATER chemical treatment, sodium carbonate are softened precipitation process and comprised the steps:
First, feeding lime and calcium chloride in first order reaction pond, utilize Ca wherein 2+and OH -with the F in waste water -and Mg 2+reaction generates CaF 2, Mg (OH ) 2flocs unit, the fluorion removed in water body has gone out magnesium ion simultaneously, utilizes coagulative precipitation device or air-floating apparatus, is separated by solid-liquid, reduce hardness concentration;
Then, the water outlet of first order reaction pond enters fluorion device, is separated by Calcium Fluoride (Fluorspan) with magnesium hydrate precipitate, and reduce fluorion and magnesium hardness concentration, water outlet enters in second order reaction pond, and second order reaction adds sodium carbonate in pond, utilizes CO wherein 3 2-with the Ca in waste water 2+reaction generates CaCO 3flocs unit, removes the calcium ion in water body; Utilize coagulative precipitation device or air-floating apparatus, solid-liquid is separated, reduce hardness concentration;
Finally, the water outlet of second order reaction pond enters in coagulative precipitation tank, carries out mud-water separation;
In first order reaction pond and second order reaction pond, add coagulating agent, described coagulating agent is the aqueous solution of chloride containing aluminium 10wt%, anionic polyacrylamide 0.1wt% simultaneously.
4. a kind of Coal Chemical Industry coking chemical waste water water resources as claimed in claim 1 and salt recovery process, it is characterized in that: in step (3), advanced oxidation processes adopts ozone+hydrogen peroxide, ozone dosage is 50mg/L, hydrogen peroxide dosage is 30mg/L, TOC degrades by these two kinds of oxygenants, and TOC is reduced to below 50mg/L.
5. a kind of Coal Chemical Industry coking chemical waste water water resources as claimed in claim 1 and salt recovery process, is characterized in that: step (7) and step (8) all utilize MVR vaporizer to carry out evaporative crystallization process.
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