CN205133326U - Salt -containing wastewater treatment system - Google Patents
Salt -containing wastewater treatment system Download PDFInfo
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- CN205133326U CN205133326U CN201520916778.7U CN201520916778U CN205133326U CN 205133326 U CN205133326 U CN 205133326U CN 201520916778 U CN201520916778 U CN 201520916778U CN 205133326 U CN205133326 U CN 205133326U
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Abstract
The utility model provides a salt -containing wastewater treatment system, this salt -containing wastewater treatment system includes the electrodialysis device for receive and handle including salt waste water, and output desalted water, membrane distillation system is connected with the electrodialysis device for receive and concentrated desalted water, the supercritical water oxidation device is connected with membrane distillation system for receive the desalted water after the concentration, and carry out oxidation treatment to the desalted water after the concentration. The utility model discloses an electrodialysis device separates containing salt waste water, and the desalted water who isolates inputs after the membrane distillation system concentration and carry out the oxidation reaction in the supercritical water oxidation device, and desalting effect is good, has avoided the corruption and the jam of salt pair supercritical water oxidation device, has protected the supercritical water oxidation device effectively, has ensured the safe operation of supercritical water oxidation device, in addition, desalted water carries out the concentration through membrane distillation system for enrichments such as the organic matter among the desalted water have improved the work efficiency of supercritical water oxidation device.
Description
Technical field
The utility model relates to technical field of waste water processing, in particular to a kind of brine waste treatment system.
Background technology
Along with the quick propelling of China's industrialization and urbanization, trade effluent rapidly increases, and has increased the weight of the pollution to earth's surface and body of groundwater, and then threatens ecological safety and residents ' health.At present, the general method of wastewater treatment part that can only process in waste water is easy to the material of biochemical degradation, but, for the waste water of a large amount of saliferous produced in the industry waste water such as printing and dyeing, papermaking, chemical industry, medicine and agricultural chemicals, high density bio-refractory, adopt general method of wastewater treatment then effectively cannot process it.
Supercritical Water Oxidation Technology (SupercriticalWaterOxidation, be called for short SCWO) is a kind of new technique to organic waste and treatment of Organic Wastewater being subject to extensive concern in recent years.The principle of supercritical Water Oxidation Technology take supercritical water as reaction medium, through the oxidizing reaction of homogeneous phase, organism is rapidly converted into CO
2, H
2o, N
2with other harmless small molecules.Utilize supercritical Water Oxidation Technology to carry out degradation treatment to organic waste water and carbon-contained organic matter, can fundamentally solve the pollution problem such as waste water, mud, thus realize innoxious, minimizing and the recycling of the pollutent such as waste water, mud.
Supercritical water in supercritical Water Oxidation Technology can dissolve each other completely with apolar substance (as hydro carbons) and other organism, and dissolve each other completely with gases such as air, oxygen, nitrogen and carbonic acid gas, but, cannot well with inorganics particularly salt dissolve each other, so just cause the salt in waste water to remain in supercritical water oxidation apparatus, cause blocking and the corrosion of supercritical water oxidation apparatus.Usually, when utilizing supercritical Water Oxidation Technology process brine waste, first desalting treatment is carried out to brine waste, the waste water of removing inorganic salt is inputed to supercritical water oxidation apparatus, utilize the organism in the oxygenizement removing waste water of supercritical water and oxygenant.But, the desalting treatment method of brine waste in prior art, as flash distillation desalination method etc., just carry out simple desalination, desalting effect is poor, the content entering the salt in the waste water of supercritical water oxidation apparatus is still very high, easily blocking and corrosion supercritical water oxidation apparatus, and then affects the safe operation of supercritical water oxidation apparatus.
Utility model content
Given this, the utility model proposes a kind of brine waste treatment system, be intended to the problem of the desalting effect difference solving brine waste in prior art.
An aspect, the utility model proposes a kind of brine waste treatment system, and this brine waste treatment system comprises: electrodialysis unit, for receiving and processing brine waste, and exports desalination water; Membrane distillation system, is connected with described electrodialysis unit, for receiving and concentrating desalination water; Supercritical water oxidation apparatus, is connected with membrane distillation system, for receiving the desalination water after concentrating, and carries out oxide treatment to the desalination water after concentrated.
Further, in above-mentioned brine waste treatment system, membrane distillation system comprises: heating unit, is connected with electrodialysis unit, for receive and heat electrodialysis unit export desalination water; Distillation device, is connected with heating unit, for receiving and concentrating the desalination water after heating.
Further, in above-mentioned brine waste treatment system, heating unit is electric heater.
Further, in above-mentioned brine waste treatment system, heating unit comprises: heat exchanger and heat pump; Wherein, the entrance of the first channel of heat exchanger is connected with the outlet of electrodialysis unit, and the outlet of the first channel of heat exchanger is connected with the entrance of distillation device; The entrance of the second passage of heat exchanger is connected with hot pump outlet, and the outlet of the second passage of heat exchanger is connected with the entrance of heat pump.
Further, in above-mentioned brine waste treatment system, heating unit is First Heat Exchanger; The entrance of the first channel of First Heat Exchanger is connected with the outlet of electrodialysis unit, and the outlet of the first channel of First Heat Exchanger is connected with the entrance of distillation device; The entrance of the second passage of First Heat Exchanger is connected with the product exit of supercritical water oxidation apparatus, and for receiving the product that supercritical oxidation device exports, the outlet of the second passage of First Heat Exchanger is used for the product after heat exchange to discharge.
Further, above-mentioned brine waste treatment system also comprises: steam-generating installation; Wherein, the liquid inlet of steam-generating installation is connected with the product exit of supercritical water oxidation apparatus, for receiving the product that supercritical water oxidation apparatus exports; The liquid exit of steam-generating installation is for exporting product; The soft water entrance of steam-generating installation is for receiving soft water; The vapour outlet of steam-generating installation is connected with the entrance of the second passage of First Heat Exchanger, for by with product heat exchange after the steam that produces export the second passage of First Heat Exchanger to.
Further, in above-mentioned brine waste treatment system, heating unit is the second interchanger; The entrance of the first channel of the second interchanger is connected with the outlet of electrodialysis unit, and the outlet of the first channel of the second interchanger is connected with the entrance of distillation device; The entrance of the second passage of the second interchanger is connected with the vapor condensation water out of distillation device, and for receiving the steam condensate that distillation device exports, the outlet of the second passage of the second interchanger is used for the steam condensate after heat exchange to discharge.
Further, above-mentioned brine waste treatment system also comprises: cold feed device; Wherein, distillation device is gap field orientation device, and gap field orientation device is connected with cold feed device, and cold feed device is used for providing water coolant for gap field orientation device.
Further, above-mentioned brine waste treatment system also comprises: negative pressure device; Wherein, distillation device is decompression type distillation device, and decompression type distillation device is connected with negative pressure device, and negative pressure device is for reducing the pressure in decompression type distillation device.
Further, above-mentioned brine waste treatment system also comprises: air mix facilities; Wherein, the entrance of air mix facilities is for receiving brine waste, the entrance of air mix facilities is also connected with the vapor condensation water out of distillation device, the outlet of air mix facilities is connected with the entrance of electrodialysis unit, and air mix facilities exports electrodialysis unit to after being mixed by the steam condensate that brine waste and distillation device export.
In the utility model, by electrodialysis unit, brine waste is separated, isolate desalination water and saliferous condensed water, desalination water inputs in supercritical water oxidation apparatus and carries out oxidizing reaction after membrane distillation system is concentrated, desalination better can be carried out to brine waste, solve the problem of the desalting effect difference of brine waste in prior art, avoid the Corrosion blockage of salt pair supercritical water oxidation apparatus, effectively protect supercritical water oxidation apparatus, ensure that the safe operation of supercritical water oxidation apparatus; In addition, desalination water is concentrated by membrane distillation system, makes the enrichments such as the organism in desalination water, improves the working efficiency of supercritical water oxidation apparatus.
Accompanying drawing explanation
By reading hereafter detailed description of the preferred embodiment, various other advantage and benefit will become cheer and bright for those of ordinary skill in the art.Accompanying drawing only for illustrating the object of preferred implementation, and is not thought restriction of the present utility model.And in whole accompanying drawing, represent identical parts by identical reference symbol.In the accompanying drawings:
The structural representation of the brine waste treatment system that Fig. 1 provides for the utility model embodiment;
The another structural representation of the brine waste treatment system that Fig. 2 provides for the utility model embodiment;
The another structural representation of the brine waste treatment system that Fig. 3 provides for the utility model embodiment;
The another structural representation of the brine waste treatment system that Fig. 4 provides for the utility model embodiment;
The another structural representation of the brine waste treatment system that Fig. 5 provides for the utility model embodiment;
The another structural representation of the brine waste treatment system that Fig. 6 provides for the utility model embodiment;
The another structural representation of the brine waste treatment system that Fig. 7 provides for the utility model embodiment;
The another structural representation of the brine waste treatment system that Fig. 8 provides for the utility model embodiment.
Embodiment
Below with reference to accompanying drawings exemplary embodiment of the present disclosure is described in more detail.Although show exemplary embodiment of the present disclosure in accompanying drawing, however should be appreciated that can realize the disclosure in a variety of manners and not should limit by the embodiment set forth here.On the contrary, provide these embodiments to be in order to more thoroughly the disclosure can be understood, and complete for the scope of the present disclosure can be conveyed to those skilled in the art.It should be noted that, when not conflicting, the embodiment in the utility model and the feature in embodiment can combine mutually.Below with reference to the accompanying drawings and describe the utility model in detail in conjunction with the embodiments.
See the structural representation of the brine waste treatment system that Fig. 1, Fig. 1 provide for the utility model embodiment.As shown in the figure, this brine waste treatment system comprises: electrodialysis unit 1, membrane distillation system 2 and supercritical water oxidation apparatus 3.Wherein, electrodialysis unit 1 for receiving and processing brine waste, and exports desalination water.Membrane distillation system 2 is connected with electrodialysis unit 1, for receiving and concentrating the desalination water that electrodialysis unit 1 exports, and export concentrated after desalination water.Supercritical water oxidation apparatus 3 is connected with membrane distillation system 2, for receive that membrane distillation system 2 exports concentrated after desalination water, and oxide treatment is carried out to desalination water after concentrated.
Particularly, electrodialysis unit 1 pair of brine waste processes, and brine waste is separated into desalination water and saliferous condensed water.The outlet of electrodialysis unit comprises desalination water outlet 120 and saliferous condensed water outlet 130, and desalination water outlet 120 is for exporting desalination water to membrane distillation system 2, and the outlet 130 of saliferous condensed water is for exporting saliferous condensed water.The entrance of supercritical water oxidation apparatus comprises desalination water entrance 31, oxidant inlet 32 and carbonaceous material entrance 33, desalination water entrance 31 for receive that membrane distillation system 2 exports concentrated after desalination water, oxidant inlet 32 is for receiving oxygenant, and carbonaceous material entrance 33 is for receiving carbonaceous material.In supercritical water oxidation apparatus 3, desalination water and oxygenant and carbonaceous material generation oxidizing reaction, produce product and the waste residue of High Temperature High Pressure.The outlet of supercritical water oxidation apparatus comprises product exit 34 and waste residue outlet 35, and product exit 34 is for exporting the product of High Temperature High Pressure, and waste residue outlet 35 is for exporting waste residue.
It should be appreciated by those skilled in the art that brine waste needs when carrying out supercritical water oxidation to pass into oxygenant and carbonaceous material, the organism generation oxidizing reaction in oxygenant and carbonaceous material and waste water is that those skilled in the art are known, therefore does not repeat.
During work, brine waste inputs to electrodialysis unit 1 by the entrance 110 of electrodialysis unit, and in electrodialysis unit 1, brine waste is separated, obtain desalination water and saliferous condensed water, the desalination water outlet 120 of electrodialysis unit exports desalination water to membrane distillation system 2.In membrane distillation system 2, a part of water in desalination water is exported by membrane distillation system 2 as a vapor, therefore makes desalination water concentrate, and then makes the enrichments such as organism in desalination water.Membrane distillation system 2 exports the desalination water after concentrated to supercritical water oxidation apparatus 3, and in supercritical water oxidation apparatus 3, desalination water and oxygenant and carbonaceous material carry out oxidizing reaction.Isolated saliferous condensed water exports by the saliferous condensed water outlet 130 of electrodialysis unit.
Can find out, in the present embodiment, be separated by electrodialysis unit 1 pair of brine waste, isolate desalination water and saliferous condensed water, desalination water inputs in supercritical water oxidation apparatus 3 and carries out oxidizing reaction after membrane distillation system 2 is concentrated, desalination better can be carried out to brine waste, solve the problem of the desalting effect difference of brine waste in prior art, avoid the Corrosion blockage of salt pair supercritical water oxidation apparatus, effectively protect supercritical water oxidation apparatus, ensure that the safe operation of supercritical water oxidation apparatus; In addition, desalination water is concentrated by membrane distillation system 2, makes the enrichments such as the organism in desalination water, improves the working efficiency of supercritical water oxidation apparatus.
Below in conjunction with Fig. 1, the present embodiment is introduced in more detail.This brine waste treatment system can also comprise pretreatment unit 13, the 3rd interchanger 14, desalting plant 15 and tripping device 16.Wherein, the entrance 131 of pretreatment unit is for receiving brine waste, the outlet 132 of pretreatment unit is connected with the entrance 110 of electrodialysis unit, the desalination water outlet 120 of electrodialysis unit is connected with the desalination water entrance 31 of supercritical water oxidation apparatus by membrane distillation system 2, the 3rd interchanger 14 successively, the saliferous condensed water outlet 130 of electrodialysis unit is connected with the waterwater entrance 151 of desalting plant, and the solid outlet 152 of desalting plant is for exporting solid salt.
Particularly, the entrance 141 of the first channel of the 3rd interchanger is connected with the outlet of membrane distillation system 2, the outlet 142 of the first channel of the 3rd interchanger is connected with the desalination water entrance 31 of supercritical water oxidation apparatus, the entrance 143 of the second passage of the 3rd interchanger is connected with the product exit 34 of supercritical water oxidation apparatus, and the outlet 144 of the second passage of the 3rd interchanger is connected with the entrance 161 of tripping device.The heat exchange after product that tripping device 16 exports for receiving the 3rd interchanger 14, and product is separated, obtain gas-phase product and liquid product, gas-phase product and liquid product export by the outlet of tripping device 16 respectively.
In the present embodiment, pretreatment unit 13 for the macrobead solid impurity in filtering salt waste water, and exports the brine waste after filtering to electrodialysis unit 1, protects electrodialysis unit 1 better.Pretreatment unit 13 can be filtering net, also can be grid, can also input flocculation agent in brine waste, the calcium magnesium plasma in removing brine waste.The desalination water of 3rd interchanger 14 to input supercritical water oxidation apparatus 3 carries out pre-heating temperature elevation, makes desalination water carry out oxidizing reaction better, guarantees efficiently carrying out of supercritical water oxidation apparatus 3.Desalting plant 15 can be evaporated crystallization device, and the moisture evaporation in the saliferous condensed water exported by electrodialysis unit 1, makes solid salt separate out.When desalting plant 15 is evaporated crystallization device, the product inlet 154 of desalting plant is connected with the outlet 144 of the second passage of the 3rd interchanger, for receiving the product after the 3rd interchanger heat exchange cooling.The product that 3rd interchanger 14 exports by desalting plant 15 and saliferous condensed water carry out heat exchange, the heat of product is made to pass to saliferous condensed water, and then saliferous condensed water is evaporated, separate out the salt in saliferous condensed water, and the solid outlet 152 of salt by desalting plant is discharged.After product and saliferous condensed water carry out heat exchange, temperature reduces and exports tripping device 16 to by the liquid exit 153 of desalting plant, then the entrance 161 of tripping device is connected with the liquid exit 153 of desalting plant, tripping device 16 receive and be separated desalting plant 15 export cooling after product, obtain gas-phase product and liquid product, and gas-phase product and liquid product are exported respectively.Product separation is gas-phase product and liquid product by tripping device 16, is convenient to recycle, and improves energy utilization rate.
During work, brine waste is inputted by the entrance 131 of pretreatment unit, macrobead solid impurity in pretreatment unit 13 filtering salt waste water, and exports the brine waste after filtering to electrodialysis unit 1 by the outlet 132 of pretreatment unit.In electrodialysis unit 1, brine waste is separated, isolate desalination water and saliferous condensed water, the desalination water outlet 120 of electrodialysis unit exports desalination water to membrane distillation system 2, desalination water concentrates in membrane distillation system 2, and exported in the first channel of the 3rd interchanger 14 by the outlet of membrane distillation system 2, wait for that heat exchange heats up; The product of the High Temperature High Pressure that supercritical water oxidation apparatus 3 exports inputs in the second passage of the 3rd interchanger 14, waits for heat exchange cooling.In the 3rd interchanger 14, desalination water after concentrated and the product of High Temperature High Pressure carry out heat exchange, desalination water temperature after concentrated raises to input in supercritical water oxidation apparatus 3 carries out oxidizing reaction, and the product temperatur of High Temperature High Pressure reduces relatively, but still there is higher temperature, then this product is inputed in desalting plant 15.Desalting plant 15 also receives the saliferous condensed water after the separation exported by electrodialysis unit 1, product heat exchange after the cooling that the outlet 144 of the second passage of this saliferous condensed water and the 3rd interchanger exports, improve the temperature of saliferous condensed water, accelerate the velocity of evaporation of saliferous condensed water, solid salt is separated out quickly.The solid salt of separating out is exported by the solid outlet 152 of desalting plant, and the solid salt after output can carry out the harmless treatment such as landfill, burning; And the temperature of product reduces again, export tripping device 16 to by the liquid exit 153 of desalting plant.Product liquid is separated by tripping device 16, obtains gas-phase product and liquid product, and gas-phase product and liquid product is exported respectively.
See Fig. 1, in above-described embodiment, this membrane distillation system 2 can comprise: heating unit 21 and distillation device 22.Wherein, heating unit 21 is connected with electrodialysis unit 1, for receive and heat electrodialysis unit 1 export desalination water.Distillation device 22 is connected with heating unit 21, for receiving and concentrating the desalination water after heating.Particularly, the entrance of heating unit 21 and the desalination water of electrodialysis unit export 120 and are connected, and the liquid inlet 221 of distillation device is connected with the outlet of heating unit 21.The outlet of distillation device comprises liquid exit 222 and vapor condensation water out 223, and liquid exit 222 is connected with the entrance 141 of the first channel of the 3rd interchanger, and vapor condensation water out 223 exports for the steam condensate will produced in distillation device.
In the present embodiment, distillation device 22 comprises hot side and produces water side.Hot side is for holding the desalination water after heating unit 21 heats exported by electrodialysis unit 1, and desalination water produces vapour transmission film and enters product water side, and steam is condensed into water in product water side, and steam condensate is exported by the vapor condensation water out 223 of distillation device.
During work, export 120 desalination waters exported by the desalination water of electrodialysis unit and input in heating unit 21 through the entrance of heating unit 21, heating unit 21 pairs of desalination waters heat, and export the desalination water after heating to distillation device 22.Distillation device 22 concentrates the desalination water after heating, a part of water in desalination water is inputed to through film as a vapor and produces water side, steam exports after product water side is condensed into steam condensate, and therefore, the water in desalination water reduces and achieves the concentrated of desalination water.Desalination water after concentrated inputs to input in supercritical water oxidation apparatus 3 after the 3rd interchanger 14 carries out heat exchange intensification and carries out oxidizing reaction.
Can find out, in the present embodiment, by heating desalination water, improve the temperature of desalination water, be convenient to desalination water and produce steam better in distillation device 22, concentrate, make the enrichments such as the organism in desalination water, the organism of enrichment carries out oxidizing reaction better in supercritical water oxidation apparatus 3, improves the working efficiency of supercritical water oxidation apparatus 3.
A kind of preferred structure of heating unit is shown see Fig. 2, Fig. 2.As shown in the figure, heating unit 21 can be electric heater 4, is heated by electric heater 4 pairs of desalination waters, and structure is simple, easy handling.
The another kind of preferred structure of heating unit is shown see Fig. 3, Fig. 3.As shown in the figure, heating unit 21 also can comprise: heat exchanger 5 and heat pump 6.Wherein, the entrance 51 of the first channel of this heat exchanger is connected with the outlet of electrodialysis unit 1, the outlet 52 of the first channel of heat exchanger is connected with the entrance of distillation device 22, the entrance 53 of the second passage of heat exchanger is connected with hot pump outlet 62, and the outlet 54 of the second passage of heat exchanger is connected with the entrance 61 of heat pump.Particularly, the entrance 51 of the first channel of this heat exchanger exports 120 with the desalination water of electrodialysis unit and is connected, and the outlet 52 of the first channel of heat exchanger is connected with the liquid inlet 221 of distillation device.Preferably, heat pump 6 is absorption heat pump, and absorption heat pump can extract extraneous water, and utilizes extraneous high temperature heat or middle low temperature heat energy to heat water, then exports hot water.Wherein, high temperature heat can be the heat of High Temperature High Pressure product that supercritical water oxidation apparatus 3 exports, and middle low temperature heat energy can be waste heat in factory or used heat.Therefore, the hot water that the heat pump 6 in the desalination water that the electrodialysis unit 1 in the first channel of heat exchanger 5 exports and second passage exports carries out heat exchange.
During work, the desalination water that the desalination water outlet 120 of electrodialysis unit exports inputs in heat exchanger 5 through the entrance 51 of the first channel of over-heat-exchanger, waits for that heat exchange heats up; High temperature heat extraneous for the water conservancy in the external world of extraction or middle low temperature heat energy heat water by heat pump 6, and are inputed to by hot water in the second passage of heat exchanger 5, wait for heat exchange cooling.In heat exchanger 5, desalination water and hot water carry out heat exchange, and the temperature of desalination water raises and inputs to distillation device 22 by the outlet 52 of the first channel of heat exchanger, and hot water temperature exports heat pump 6 to and proceeds heating after reducing, repeat aforesaid operations.
Can find out, in the present embodiment, the hot water produced by heat pump and desalination water carry out heat exchange, improve the temperature of desalination water, take full advantage of the extraneous energy.
Another preferred structure of heating unit is shown see Fig. 4, Fig. 4.As shown in the figure, heating unit 21 also can be First Heat Exchanger 7.Wherein, the entrance 71 of the first channel of First Heat Exchanger is connected with the outlet of electrodialysis unit, and the outlet 72 of the first channel of First Heat Exchanger is connected with the entrance of distillation device; The entrance 73 of the second passage of First Heat Exchanger is connected with the product exit 34 of supercritical water oxidation apparatus, for receiving the product that supercritical oxidation device 3 exports, the outlet 74 of the second passage of First Heat Exchanger is for discharging the product after heat exchange, then the product that the supercritical oxidation device 3 in the desalination water that the electrodialysis unit 1 in the first channel of First Heat Exchanger 7 exports and second passage exports carries out heat exchange.Particularly, the entrance 71 of the first channel of First Heat Exchanger exports 120 with the desalination water of electrodialysis unit and is connected, and the outlet 72 of the first channel of First Heat Exchanger is connected with the liquid inlet 221 of distillation device.The outlet 74 of the second passage of First Heat Exchanger is connected with the product inlet 154 of desalting plant, for exporting the product after heat exchange cooling in the second passage of First Heat Exchanger to desalting plant 15.
In the present embodiment, the product of the High Temperature High Pressure that supercritical water oxidation apparatus 3 exports can be divided into two-way to export, one tunnel exports in the 3rd interchanger 14 carries out heat exchange, another road exports in First Heat Exchanger 7 carries out heat exchange, 3rd interchanger 14 and First Heat Exchanger 7 all export the product after heat exchange to desalting plant 15, take full advantage of the heat of the product that supercritical water oxidation apparatus 3 exports, avoid the waste of heat, improve energy utilization rate.
During work, the desalination water that the desalination water outlet 120 of electrodialysis unit exports inputs in the first channel of First Heat Exchanger 7 through the entrance 71 of the first channel of First Heat Exchanger, waits for that heat exchange heats up; A part in the product of the High Temperature High Pressure of product exit 34 output of supercritical water oxidation apparatus exports in the 3rd interchanger 14 carries out heat exchange, and another part then exports in the second passage of First Heat Exchanger 7, waits for heat exchange cooling.In First Heat Exchanger 7, the product of desalination water and High Temperature High Pressure carries out heat exchange, and the temperature of desalination water raises and inputs to distillation device 22 by the outlet 72 of the first channel of First Heat Exchanger, and the product temperatur of High Temperature High Pressure reduces, and exports desalting plant 15 to.In desalting plant 15, the product after cooling and saliferous condensed water carry out heat exchange cooling, then the product after cooling are again inputed in tripping device 16 and are separated.
Can find out, in the present embodiment, take full advantage of the energy, improve the utilization ratio of the energy.
See the another structural representation of the brine waste treatment system that Fig. 5, Fig. 5 provide for the utility model embodiment.As shown in the figure, in the above-described embodiments, heating unit 21 can also comprise: steam-generating installation 8.Wherein, the liquid inlet 81 of this steam-generating installation is connected with the product exit 34 of supercritical water oxidation apparatus, for receiving the product that supercritical water oxidation apparatus 3 exports; The liquid exit 84 of steam-generating installation is for exporting product.The soft water entrance 82 of steam-generating installation is for receiving soft water; The vapour outlet 83 of steam-generating installation is connected with the entrance 73 of the second passage of First Heat Exchanger, for by with product heat exchange after the steam that produces export the second passage of First Heat Exchanger 7 to.
Particularly, the liquid exit 84 of steam-generating installation is connected with the entrance 143 of the second passage of the 3rd interchanger.Soft water can be extraneous soft water system, also can be the steam condensate that the vapor condensation water out 223 of distillation device exports.Steam-generating installation 8 can be vapour generator, and preferably, steam-generating installation 8 is heat pipe evaporator.
During work, the product of the High Temperature High Pressure of product exit 34 output of supercritical water oxidation apparatus inputs in steam-generating installation 8 through the liquid inlet 81 of steam-generating installation, and soft water is inputed in steam-generating installation 8 by the soft water entrance 82 of steam-generating installation.In steam-generating installation 8, the high temperature of the product utilizing supercritical water oxidation apparatus to export and soft water heat exchange, soft water is evaporated, produces the steam with certain pressure and temperature, the interior desalination water exported with electrodialysis unit 1 of second passage that steam exports First Heat Exchanger 7 to carries out heat exchange cooling; And the temperature of product after heat exchange reduces relatively, by the liquid exit 84 of steam-generating installation export to export with distillation device 22 in the 3rd interchanger 14 concentrated after desalination water proceed heat exchange.
Can find out, in the present embodiment, the product of the High Temperature High Pressure utilizing supercritical water oxidation apparatus 3 to export makes soft water generates steam, recycle the desalination water that this steam and electrodialysis unit 1 export and carry out heat exchange, then the heats of desalination water is better, and then is conducive to the concentrated of distillation device 22 pairs of desalination waters.
Another preferred structure of heating unit is shown see Fig. 6, Fig. 6.As shown in the figure, heating unit 21 also can be the second interchanger 9.Wherein, the entrance 91 of the first channel of the second interchanger is connected with the outlet of electrodialysis unit 1, and the outlet 92 of the first channel of the second interchanger is connected with the entrance of distillation device; The entrance 93 of the second passage of the second interchanger is connected with the vapor condensation water out 223 of distillation device, for receiving the steam condensate that distillation device 22 exports, the outlet 94 of the second passage of the second interchanger is for discharging the steam condensate after heat exchange, then the steam condensate that the distillation device 22 in the desalination water that the electrodialysis unit 1 in the first channel of the second interchanger exports and second passage exports carries out heat exchange.Particularly, the entrance 91 of the first channel of the second interchanger exports 120 with the desalination water of electrodialysis unit and is connected, and the outlet 92 of the first channel of the second interchanger is connected with the liquid inlet 221 of distillation device.
During work, the desalination water that the desalination water outlet 120 of electrodialysis unit exports inputs in the first channel of the second interchanger 9 through the entrance 91 of the first channel of the second interchanger, waits for that heat exchange heats up; Produce the steam condensate in water side in distillation device 22, still have certain temperature, steam condensate exports in the second passage of the second interchanger 9 by vapor condensation water out 223, waits for heat exchange cooling.In the second interchanger 9, desalination water and steam condensate carry out heat exchange, the temperature of desalination water raises and inputs to distillation device 22 by the outlet 92 of the first channel of the second interchanger, and the temperature of steam condensate reduces, and is exported by the outlet 94 of the second passage of the second interchanger.
Can find out, in the present embodiment, the desalination water that the steam condensate exported by distillation device 22 and electrodialysis unit 1 are exported carries out heat exchange, takes full advantage of the heat of the steam condensate that distillation device 22 exports, improves the utilization ratio of the energy.
A kind of preferred structure of distillation device is shown see Fig. 7, Fig. 7.As shown in the figure, in the various embodiments described above, this brine waste treatment system can also comprise: cold feed device 10.Wherein, distillation device 22 is gap field orientation device, gap field orientation device is connected with cold feed device 10, cold feed device 10 is for providing cold water for gap field orientation device, make the steam that in gap field orientation device, desalination water produces carry out condensation better in product water side, improve the working efficiency of gap field orientation device.
It should be appreciated by those skilled in the art that in the present embodiment, gap field orientation device comprises hot side, cold side and product water side, produces water and is placed between hot side and cold side.Hot side is for holding the desalination water after heating unit 21 heats exported by electrodialysis unit 1, cold side is for holding water coolant, the vapour transmission film that desalination water in hot side produces enters and produces water side, steam carries out heat exchange with the water coolant of cold side in product water side, produce steam condensate, steam condensate is exported by vapor condensation water out 223.
In the present embodiment, cold feed device 10 comprises refrigerating unit 101 and cold water storage device 102, the entrance 1021 of cold water storage device is for receiving water coolant, the outlet 1022 of cold water storage device is connected with the cold side input port 224 of gap field orientation device, the cold side outlet port 225 of gap field orientation device is connected with the entrance 1011 of refrigerating unit, and the outlet 1012 of refrigerating unit is connected with the entrance 1021 of cold water storage device.Cold water storage device 102 also can receive the water coolant that the external world provides, and is convenient to timely, supplements water coolant better, and change the water coolant stored.
During work, the water coolant stored in it is inputed to the cold side of gap field orientation device by cold water storage device 102, the water coolant that the vapour transmission film that desalination water in the hot side of gap field orientation device produces is producing water side and cold side carries out heat exchange, vapor condensation is water, the temperature of the water coolant of cold side raises gradually, exported in refrigerating unit 101 by the cold side outlet port 225 of gap field orientation device and carry out cooling down, water coolant after cooling is exported in cold water storage device 102 by the outlet 1012 of refrigerating unit and stores, so that follow-up use.
Can find out, in the present embodiment, distillation device 22 is gap field orientation device, by producing the steam of water side in cold gas gap type distillation device, accelerate the speed of the vapor condensation of gap field orientation device, improve the stability of gap field orientation device.
The another kind of preferred structure of distillation device is shown see Fig. 8, Fig. 8.As shown in the figure, in the various embodiments described above, this brine waste treatment system can also comprise: negative pressure device 11.Wherein, distillation device 22 is decompression type distillation device, and decompression type distillation device is connected with negative pressure device 11, and negative pressure device 11 is for reducing the pressure in decompression type distillation device.
It should be appreciated by those skilled in the art that decompression type distillation device comprises hot side and produces water side.Hot side exports 120 desalination waters after heating unit 21 heats exported for holding by the desalination water of electrodialysis unit, the vapour transmission film that desalination water produces enters and produces water side, under the effect of negative pressure device 11, steam exports by producing water side, and the pressure produced in water side is reduced.
Particularly, negative pressure device 11 comprises vapor condensation water collecting device 111 and vacuum pump 112.The entrance 1111 of vapor condensation water collecting device can be connected with the outlet of the product water side of decompression type distillation device, for collecting the steam producing water side and export.The entrance 1111 of vapor condensation water collecting device also can be connected with the outlet 94 of the second passage of the second interchanger, for collecting the steam condensate that the second interchanger 9 exports.The outlet 1112 of vapor condensation water collecting device is connected with vacuum pump 112, and vacuum pump 112 produces the steam of water side in decompression type distillation device for extracting, to reduce the pressure producing water side.
See Fig. 8, in the present embodiment, in order to make full use of the energy, the entrance 1111 of vapor condensation water collecting device is connected with the outlet 94 of the second passage of the second interchanger, decompression type distillation device produces the steam of water side output first after the second interchanger 9 heat exchange cooling total condensation is water, input to again in vapor condensation water collecting device 111 and store, so that follow-up use.
It should be noted that, the vapour transmission film that in decompression type distillation device, the desalination water of hot side produces enters and produces water side, steam product water side in a part be condensed into water, still some exists as a vapor, thus by vapor condensation export export be gas-liquid mixture.
During work, the desalination water generates steam of hot side in decompression type distillation device, vapour transmission film enters and produces water side, under the effect of vacuum pump 112, gas-liquid mixture exports in the second passage of the second interchanger by vapor condensation water out 223, heat exchange is carried out with the desalination water in input decompression type distillation device in the second interchanger 9, then after desalination water heat exchange, temperature raises the hot side inputing to decompression type distillation device, after gas-liquid mixture heat exchange, temperature reduces total condensation is that water is exported in vapor condensation water collecting device 111 by the outlet 94 of the second passage of the second interchanger and stores.
Can find out, in the present embodiment, water distilling apparatus is decompression type distillation device, by the steam in vacuum pump extraction product water side to reduce the pressure producing water side in distillation device, accelerate the speed of the vapour transmission film of decompression type distillation device, improve the stability of decompression type distillation device.
See Fig. 2, in the various embodiments described above, this brine waste treatment system can also comprise: air mix facilities 12.Wherein, the entrance of this air mix facilities is for receiving brine waste, the entrance of air mix facilities is also connected with the vapor condensation water out 223 of distillation device, the outlet 122 of air mix facilities is connected with the entrance of electrodialysis unit 1, and air mix facilities 12 is for exporting electrodialysis unit 1 to by after the steam condensate exported in brine waste and distillation device mixed diluting.Particularly, the first entrance 121 of air mix facilities is connected with the outlet 132 of pretreatment unit, and the second entrance 123 of air mix facilities is connected with the vapor condensation water out 223 of distillation device.Air mix facilities 12 can be container, and brine waste and steam condensate all input in air mix facilities 12 and mix.
During work, brine waste exports air mix facilities 12 to by the outlet 132 of pretreatment unit after pre-treatment.The steam condensate producing water side in distillation device 22 exports air mix facilities 12 to by the vapor condensation water out 223 of distillation device, and wherein, steam condensate is pure water.In air mix facilities 12, brine waste mixes with steam condensate, because steam condensate is pure water, so steam condensate serves the effect of dilution to brine waste.Brine waste after dilution exports electrodialysis unit 1 to by the outlet 122 of air mix facilities.
Can find out; in the present embodiment, by air mix facilities, brine waste is diluted, make the brine waste inputing to electrodialysis unit 1 can meet the requirement of electrodialysis unit 1 pair of water quality better; improve the working efficiency of electrodialysis unit 1, and protect electrodialysis unit 1.
In sum, the present embodiment, by electrodialysis unit, brine waste is separated, isolate desalination water and saliferous condensed water, desalination water inputs in supercritical water oxidation apparatus and carries out oxidizing reaction after membrane distillation system is concentrated, can carry out desalination better, avoid the Corrosion blockage of salt pair supercritical water oxidation apparatus to brine waste, effectively protect supercritical water oxidation apparatus, ensure that the safe operation of supercritical water oxidation apparatus; In addition, desalination water is concentrated by membrane distillation system, makes the enrichments such as the organism in desalination water, improves the working efficiency of supercritical water oxidation apparatus.
Obviously, those skilled in the art can carry out various change and modification to the utility model and not depart from spirit and scope of the present utility model.Like this, if these amendments of the present utility model and modification belong within the scope of the utility model claim and equivalent technologies thereof, then the utility model is also intended to comprise these change and modification.
Claims (10)
1. a brine waste treatment system, is characterized in that, comprising:
Electrodialysis unit (1), for receiving and processing brine waste, and exports desalination water;
Membrane distillation system (2), is connected with described electrodialysis unit (1), for receiving and concentrating described desalination water;
Supercritical water oxidation apparatus (3), is connected with described membrane distillation system (2), for receiving the described desalination water after concentrating, and carries out oxide treatment to the described desalination water after concentrated.
2. brine waste treatment system according to claim 1, is characterized in that, described membrane distillation system (2) comprising:
Heating unit (21), is connected with described electrodialysis unit (1), for receive and heat described electrodialysis unit export desalination water;
Distillation device (22), is connected with described heating unit (21), for receiving and concentrating the described desalination water after heating.
3. brine waste treatment system according to claim 2, is characterized in that, described heating unit (21) is electric heater (4).
4. brine waste treatment system according to claim 2, is characterized in that, described heating unit (21) comprising: heat exchanger (5) and heat pump (6); Wherein,
The entrance (51) of the first channel of described heat exchanger is connected with the outlet of described electrodialysis unit (1), and the outlet (52) of the first channel of described heat exchanger is connected with the entrance of described distillation device (22);
The entrance (53) of the second passage of described heat exchanger is connected with the outlet of described heat pump (6), and the outlet (54) of the second passage of described heat exchanger is connected with the entrance of described heat pump (6).
5. brine waste treatment system according to claim 2, is characterized in that, described heating unit (21) is First Heat Exchanger (7);
The entrance (71) of the first channel of described First Heat Exchanger is connected with the outlet of described electrodialysis unit (1), and the outlet (72) of the first channel of described First Heat Exchanger is connected with the entrance of described distillation device (22);
The entrance (73) of the second passage of described First Heat Exchanger is connected with the product exit of described supercritical water oxidation apparatus (3), for receiving the product that described supercritical oxidation device (3) exports, the outlet (74) of the second passage of described First Heat Exchanger is for discharging the described product after heat exchange.
6. brine waste treatment system according to claim 5, is characterized in that, also comprise: steam-generating installation (8); Wherein,
The liquid inlet (81) of described steam-generating installation is connected with the product exit (34) of described supercritical water oxidation apparatus, for receiving the product that described supercritical water oxidation apparatus (3) exports; The liquid exit (84) of described steam-generating installation is for exporting product;
The soft water entrance (82) of described steam-generating installation is for receiving soft water; The vapour outlet (83) of described steam-generating installation is connected with the entrance (73) of the second passage of described First Heat Exchanger, for by with described product heat exchange after the steam that produces export the second passage of described First Heat Exchanger (7) to.
7. brine waste treatment system according to claim 2, is characterized in that, described heating unit (21) is the second interchanger (9);
The entrance (91) of the first channel of described second interchanger is connected with the outlet of described electrodialysis unit (1), and the outlet (92) of the first channel of described second interchanger is connected with the entrance of described distillation device (22);
The entrance (93) of the second passage of described second interchanger is connected with the vapor condensation water out of described distillation device (22), for receiving the steam condensate that described distillation device (22) exports, the outlet (94) of the second passage of described second interchanger is for discharging the described steam condensate after heat exchange.
8. the brine waste treatment system according to any one of claim 2 to 7, is characterized in that, also comprise: cold feed device (10); Wherein,
Described distillation device (22) is gap field orientation device, described gap field orientation device is connected with described cold feed device (10), and described cold feed device (10) is for providing water coolant for described gap field orientation device.
9. the brine waste treatment system according to any one of claim 2 to 7, is characterized in that, also comprise: negative pressure device (11); Wherein,
Described distillation device is (22) decompression type distillation device, described decompression type distillation device is connected with described negative pressure device (11), and described negative pressure device (11) is for reducing the pressure in described decompression type distillation device.
10. brine waste treatment system according to claim 2, is characterized in that, also comprise: air mix facilities (12); Wherein,
The entrance of described air mix facilities (12) is for receiving brine waste, the entrance of described air mix facilities (12) is also connected with the vapor condensation water out of described distillation device (22), the outlet of described air mix facilities (12) is connected with the entrance of described electrodialysis unit (1), and described air mix facilities (12) exports described electrodialysis unit (1) to after mixing for the steam condensate described brine waste and described distillation device exported.
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| CN201520916778.7U CN205133326U (en) | 2015-11-17 | 2015-11-17 | Salt -containing wastewater treatment system |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106007110A (en) * | 2016-06-17 | 2016-10-12 | 浙江奇彩环境科技股份有限公司 | Low-salt wastewater recycled treatment and recycling method |
| CN110173918A (en) * | 2019-04-30 | 2019-08-27 | 东南大学 | The device of ammonium hydroxide bromine jet type heat pump performance is promoted based on electric drive membrane separation technique |
| CN111233238A (en) * | 2020-02-08 | 2020-06-05 | 南京霄祥工程技术有限公司 | Zero-emission treatment method and device for coal chemical industry wastewater |
| CN112321051A (en) * | 2020-11-01 | 2021-02-05 | 自然资源部天津海水淡化与综合利用研究所 | Multi-membrane coupling process and device for space station wastewater treatment |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106007110A (en) * | 2016-06-17 | 2016-10-12 | 浙江奇彩环境科技股份有限公司 | Low-salt wastewater recycled treatment and recycling method |
| CN110173918A (en) * | 2019-04-30 | 2019-08-27 | 东南大学 | The device of ammonium hydroxide bromine jet type heat pump performance is promoted based on electric drive membrane separation technique |
| CN111233238A (en) * | 2020-02-08 | 2020-06-05 | 南京霄祥工程技术有限公司 | Zero-emission treatment method and device for coal chemical industry wastewater |
| CN111233238B (en) * | 2020-02-08 | 2022-04-29 | 中煤（北京）环保工程有限公司 | Zero-emission treatment method and device for coal chemical industry wastewater |
| CN112321051A (en) * | 2020-11-01 | 2021-02-05 | 自然资源部天津海水淡化与综合利用研究所 | Multi-membrane coupling process and device for space station wastewater treatment |
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