CN203954705U - A kind of chlorate/perchlorate vacuum and low temperature evaporation and crystallization system - Google Patents
A kind of chlorate/perchlorate vacuum and low temperature evaporation and crystallization system Download PDFInfo
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- CN203954705U CN203954705U CN201420406393.1U CN201420406393U CN203954705U CN 203954705 U CN203954705 U CN 203954705U CN 201420406393 U CN201420406393 U CN 201420406393U CN 203954705 U CN203954705 U CN 203954705U
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- Prior art keywords
- chlorate
- perchlorate
- crystallizing evaporator
- pump
- heat exchanger
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- XTEGARKTQYYJKE-UHFFFAOYSA-M Chlorate Chemical compound [O-]Cl(=O)=O XTEGARKTQYYJKE-UHFFFAOYSA-M 0.000 title claims abstract description 103
- VLTRZXGMWDSKGL-UHFFFAOYSA-M perchlorate Chemical compound [O-]Cl(=O)(=O)=O VLTRZXGMWDSKGL-UHFFFAOYSA-M 0.000 title claims abstract description 68
- 238000002425 crystallisation Methods 0.000 title claims abstract description 31
- 230000008025 crystallization Effects 0.000 title claims abstract description 31
- 238000001704 evaporation Methods 0.000 title claims abstract description 23
- 230000008020 evaporation Effects 0.000 title claims abstract description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 69
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 28
- 238000010438 heat treatment Methods 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims description 31
- 239000000463 material Substances 0.000 claims description 24
- 238000001816 cooling Methods 0.000 claims description 20
- 238000007599 discharging Methods 0.000 claims description 15
- 238000004062 sedimentation Methods 0.000 claims description 12
- 229910001220 stainless steel Inorganic materials 0.000 claims description 7
- 239000010935 stainless steel Substances 0.000 claims description 7
- 229910000885 Dual-phase steel Inorganic materials 0.000 claims description 5
- 238000006243 chemical reaction Methods 0.000 abstract description 11
- 239000003245 coal Substances 0.000 abstract description 10
- 238000009835 boiling Methods 0.000 abstract description 7
- 238000003912 environmental pollution Methods 0.000 abstract description 6
- 230000036647 reaction Effects 0.000 abstract description 6
- VLTRZXGMWDSKGL-UHFFFAOYSA-N perchloric acid Chemical compound OCl(=O)(=O)=O VLTRZXGMWDSKGL-UHFFFAOYSA-N 0.000 description 42
- 239000012153 distilled water Substances 0.000 description 11
- 238000000034 method Methods 0.000 description 11
- BZSXEZOLBIJVQK-UHFFFAOYSA-N 2-methylsulfonylbenzoic acid Chemical compound CS(=O)(=O)C1=CC=CC=C1C(O)=O BZSXEZOLBIJVQK-UHFFFAOYSA-N 0.000 description 8
- 239000000567 combustion gas Substances 0.000 description 7
- 239000010842 industrial wastewater Substances 0.000 description 7
- 238000009833 condensation Methods 0.000 description 5
- 230000005494 condensation Effects 0.000 description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 238000005406 washing Methods 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical group [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 229910052719 titanium Inorganic materials 0.000 description 3
- 239000010936 titanium Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000012452 mother liquor Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- BAZAXWOYCMUHIX-UHFFFAOYSA-M sodium perchlorate Chemical compound [Na+].[O-]Cl(=O)(=O)=O BAZAXWOYCMUHIX-UHFFFAOYSA-M 0.000 description 2
- 229910001488 sodium perchlorate Inorganic materials 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- ZCDOYSPFYFSLEW-UHFFFAOYSA-N chromate(2-) Chemical compound [O-][Cr]([O-])(=O)=O ZCDOYSPFYFSLEW-UHFFFAOYSA-N 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- -1 timber Substances 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a kind of chlorate/perchlorate vacuum and low temperature evaporation and crystallization system, comprise the vacuum unit connecting successively, surface condenser, crystallizing evaporator, interior circulation axial-flow pump and feed pump, crystallizing evaporator is connected with heating circulation system, heating circulation system comprises heat cycles pump and the heat exchanger connecting successively, heat exchanger is connected with interior circulation axial-flow pump by circulating line, heat exchanger is also connected with chlorate/perchlorate electrolysis unit, surface condenser bottom is provided with condensating water outlet tube, condensating water outlet tube successively with condensed water storage tank, condensate pump connects.By vacuum unit is set, be connected with crystallizing evaporator, reduce chlorate/perchlorate solution boiling point, and then required external heat reduce; By heat exchanger, be connected with chlorate/perchlorate electrolysis unit, the heat that cell reaction produces, as crystallizing evaporator external heat source, is banned boiler, and the uses such as coal, avoid environmental pollution, and the steam that crystallizing evaporator produces simultaneously is effectively recycled.
Description
Technical field
The utility model belongs to technical field of chemical, specifically refers to a kind of chlorate/perchlorate vacuum and low temperature evaporation and crystallization system.
Background technology
Original evaporative crystallization technology, chlorate/perchlorate is produced and is adopted high temperature evaporation crystallization crystal, the principle that this method is produced is that the temperature of solution is heated to boiling temperature, solvent reduces and crystallize out, this method needs the high temperature energy, and energy consumption is high, and the product of producing exists particle tiny, moisture, chromate content are high, easily the technological deficiency such as caking.
Current high temperature evaporation crystallization technique, the high temperature energy adopting generally derives from fire coal, combustion gas, timber, boiler and electric boiler etc., wherein, fire coal, combustion gas, timber, boiler and electric boiler Meteorological, operating cost and maintenance cost are high, and the impact of the use environmental pollution of fire coal, combustion gas, timber is large, and security risk is large.Meanwhile, in existing high temperature evaporation crystallization technique, after the disproportionated reaction heat energy that the electrolysis of chlorate/perchlorate produces cools by cold water, directly enter atmosphere, fail to recycle, cause energy waste.
Utility model content
The purpose of this utility model is: overcome the above-mentioned defect of prior art, ban boiler investment, save the fuel sources such as coal, combustion gas, timber, avoid environmental pollution, reduce risk factor, make full use of chlorate/perchlorate vacuum and low temperature evaporation and crystallization system of the disproportionated reaction heat of perchlorate electrolysis generation.
The utility model is achieved through the following technical solutions: comprise the vacuum unit, surface condenser, crystallizing evaporator, interior circulation axial-flow pump and the feed pump that connect successively, crystallizing evaporator is connected with heating circulation system, heating circulation system comprises heat cycles pump and the heat exchanger connecting successively, heat exchanger is connected with interior circulation axial-flow pump by circulating line, heat exchanger is also connected with chlorate/perchlorate electrolysis unit, surface condenser bottom is provided with condensating water outlet tube, and condensating water outlet tube is connected with condensed water storage tank, condensate pump successively.
The utility model is by starting vacuum unit, and vacuum unit is connected with crystallizing evaporator, reduces the interior pressure of crystallizing evaporator, thereby reduction chlorate/perchlorate solution boiling point reaches the object of crystalline product and concentrated mother liquor; By the setting of heating circulation system, the thin brilliant liquid producing in chlorate/perchlorate evaporating concentration process in crystallizing evaporator is delivered to heat exchanger by heat cycles pump, the heat that in chlorate/perchlorate electrolysis unit, cell reaction produces is sent to heat exchanger, in heat exchanger, be provided with heat exchanger tube, when thin brilliant liquid exchanges and obtains heat from heat exchanger tube as heat transferring medium, then through circulating line, be delivered to interior circulation axial-flow pump, enter in the evaporimeter in crystallizing evaporator and continue to concentrate, crystallization; By the setting of vacuum unit, perchlorate, solution of chlorate boiling point reduce, thereby the needed external heat source energy of evaporative crystallization reduces, and vacuum unit is directly discharged the incoagulable gas that enters surface condenser from crystallizing evaporator.In the utility model, pass through the combination of vacuum unit and chlorate/perchlorate electrolysis unit, the heat energy that in chlorate/perchlorate electrolysis unit, electrolysis disproportionated reaction produces is used as the external heat source of perchlorate evaporative crystallization, avoid adopting boiler, fire coal etc., reduce production costs, avoid the environmental pollution bringing thus simultaneously, and the disproportionated reaction heat that the electrolysis of chlorate/perchlorate electrolysis unit produces is just in time fully utilized, and avoids energy waste, by the setting of surface condenser, the indirect steam that crystallizing evaporator is produced is condensed into distilled water, condensed distilled water contains micro-impurity, can not directly arrange outward, it can be delivered to condensed water storage tank by being arranged on the condensating water outlet tube of surface condenser bottom, by condensate pump, use it for and dissolve Nacl as required, dissolve sodium chlorate etc., or as sodium chlorate centrifuge washings etc., the recycling of realization to industrial wastewater, reduce the pollution of industrial wastewater to environment, the common practise that other structures of the present utility model and principle thereof are affiliated field, repeat no more.
Further, described crystallizing evaporator cavity bottom is provided with material sedimentation chamber, material sedimentation chamber is communicated with discharging pump by being located at the discharging opening of its chamber wall, chlorate/perchlorate solution is in evaporating concentration process, form the crystallizing layer of different densities, the closer to crystallizing evaporator bottom, be that crystallizing layer density in material sedimentation chamber is larger, according to the requirement of chlorate/perchlorate evaporative crystallization product, the crystalline product that is positioned at material sedimentation chamber is that magma liquid passes through discharging opening, discharging pump is carried, and enters centrifugal separation system.
Further, described surface condenser one end is provided with circulating water outlet pipe, circulating water outlet pipe is connected with cooling tower, cooling tower is connected with the circulating water intake pipe that is located at surface condenser one end by water circulating pump, circulating water outlet pipe, circulating water intake Guan Jun is positioned at the same one end of surface condenser, the indirect steam that crystallizing evaporator produces enters surface condenser and is condensed into distilled water, the heat of distilled water condensation passes to the recirculated water in tubulation by the tubulation in surface condenser, recirculated water enters cooling tower through circulating water outlet pipe, cooling tower is provided with blower fan, the heat that recirculated water is carried is dispersed in atmosphere by cooling tower fan, recirculated water after cooling tower cooling enters surface condenser by water circulating pump, continue the steam that condensation enters surface condenser, realizing recirculated water reuses, and the steam heat that crystallizing evaporator is produced is taken out of.
Further, described crystallizing evaporator comprises evaporimeter and crystallizer, and crystallizer is positioned at evaporimeter lower end, and crystallizer tube wall is provided with thin brilliant liquid outlet.
Further, described thin brilliant liquid outlet is connected with heat cycles pump by circulating line, the thin brilliant liquid producing through evaporation and concentration in crystallizer in crystallizing evaporator, by heat cycles pump, be delivered to heat exchanger, in heat exchanger, heat is obtained in exchange, the heat energy that the cell reaction of origin of heat in perchlorate electrolysis unit produces, thin brilliant liquid enters interior circulation axial-flow pump by circulating line, by interior circulation axial-flow pump, carry the evaporimeter in crystallizing evaporator to proceed evaporation and concentration thin brilliant liquid, thin brilliant liquid in obtaining the process of heat energy in heat exchanger, the heat producing with chlorate/perchlorate electrolysis unit exchanges, the heat producing by the electrolysis of chlorate/perchlorate is as the external heat source of evaporative crystallization, thereby reduce boiler investment, save coal, combustion gas, the fuel sources such as timber, the flue gas of avoiding boiler operatiopn to produce, scarp contaminated environment.
Further, described crystallizing evaporator material is 316L or dual phase steel stainless steel, crystallizing evaporator carries out evaporative crystallization under hot conditions, if the material of crystallizing evaporator is stainless steel, chlorate/perchlorate can produce corrosion to crystallizing evaporator, now, crystallizing evaporator moves under the condition of 100 ℃, the material of crystallizing evaporator is titanium material, increased greatly the Meteorological of equipment, when reduce the pressure of crystallizing evaporator by vacuum unit, and then the required heat energy of reduction solution evaporative crystallization, under cryogenic conditions, carry out evaporative crystallization, chlorate/perchlorate reduces the corrosivity of crystallizing evaporator, now, the preferred 316L of material or dual phase steel stainless steel, not only reduced the corrosivity to crystallizing evaporator, and equipment cost reduces greatly.
Further, described heat exchanger is serpentine coil formula heat exchanger, in order effectively to realize thin brilliant liquid, as heat transferring medium, in heat exchanger, carry out heat exchange, in heat exchanger, be provided with serpentine coil formula heat exchanger tube, increase the contact area of heat transferring medium and heat exchanger tube, accelerate heat exchange efficiency, the heat energy that in serpentine coil formula heat exchanger tube, the electrolysis of sodium chlorate/sodium perchlorate produces is as the external heat source of the heat transferring mediums such as thin brilliant liquid, and the thin brilliant liquid after heat exchange is proceeded condensing crystallizing by the evaporimeter delivering in crystallizing evaporator of interior circulation axial-flow pump.
The utility model compared with prior art, has the following advantages and beneficial effect:
(1) the utility model is by the setting of vacuum unit, and vacuum system is connected with crystallizing evaporator, reduces pressure in crystallizing evaporator, and then reduction chlorate, perchlorate solution boiling point, the required reduction of the energy as crystallizing evaporator external heat source;
(2) the utility model is by arranging heating circulation system, heat exchanger in heating circulation system is connected with chlorate/perchlorate electrolysis unit, the heat that the cell reaction of chlorate/perchlorate electrolysis unit produces is just in time as the required external heat source of crystallizing evaporator, thereby ban boiler investment, save the use of the fuel sources such as coal, combustion gas, timber, flue gas, the scarp of having avoided boiler operatiopn to produce, cause environmental pollution;
(3) the utility model is by the setting of surface condenser, the steam that crystallizing evaporator is produced carries out condensation recovery, by the cooling heat discharge atmosphere that recirculated water is taken out of of cooling tower, condensed distilled water can be used as sodium chlorate centrifuge washings or dissolves Nacl, solid sodium chlorate etc., the recycling of realization to industrial wastewater, using water wisely, and reduce the pollution of industrial wastewater to environment, avoided directly steam being entered to atmosphere in conventional process device, caused the wasting of resources.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model;
Wherein: 1-vacuum unit, 2-surface condenser, 3-crystallizing evaporator, 4-interior circulation axial-flow pump, 5-feed pump, 6-heat cycles pump, 7-heat exchanger, 8-discharging pump, 9-cooling tower, 10-water circulating pump, 11-condensed water storage tank, 12-condensate pump, 13-material sedimentation chamber, 14-discharging opening, 15-thin brilliant liquid outlet, 16-chlorate/perchlorate electrolysis unit.
The specific embodiment
Below in conjunction with embodiment, the utility model is described in further detail, but embodiment of the present utility model is not limited to this.
Embodiment 1:
The primary structure of the present embodiment, as shown in Figure 1, comprise the vacuum unit 1, surface condenser 2, crystallizing evaporator 3, interior circulation axial-flow pump 4 and the feed pump 5 that connect successively, crystallizing evaporator 3 is connected with heating circulation system, heating circulation system comprises heat cycles pump 6 and the heat exchanger 7 connecting successively, heat exchanger 7 is connected with interior circulation axial-flow pump 4 by circulating line, heat exchanger 7 is also connected with chlorate/perchlorate electrolysis unit 16, surface condenser 2 bottoms are provided with condensating water outlet tube, and condensating water outlet tube is connected with condensed water storage tank 11, condensate pump 12 successively.The utility model is by starting vacuum unit 1, and vacuum unit 1 is connected with crystallizing evaporator 3, and then the interior pressure of reduction crystallizing evaporator 3, thus reduction chlorate, perchlorate solution boiling point, and then reach the object of crystalline product and concentrated mother liquor; By the setting of heating circulation system, the thin brilliant liquid producing in the interior chlorate/perchlorate of crystallizing evaporator 3 evaporating concentration process is delivered to heat exchanger 7 by heat cycles pump 6, in chlorate/perchlorate electrolysis unit, the heat of cell reaction is sent to heat exchanger 7, in heat exchanger 7, be provided with heat exchanger tube, when thin brilliant liquid exchanges and obtains heat from heat exchanger tube as heat transferring medium, then through circulating line, be delivered to interior circulation axial-flow pump 4, enter in crystallizing evaporator 3 evaporimeters and proceed to concentrate, crystallization; By the setting of vacuum unit 1, chlorate/perchlorate solution boiling point reduces, thereby the needed external heat source temperature of evaporative crystallization reduces.In the utility model, pass through the combination of vacuum unit 1 and chlorate/perchlorate electrolysis unit 16, the heat energy that in chlorate/perchlorate electrolysis unit 16, electrolysis disproportionated reaction produces is used as the external heat source of chlorate/perchlorate evaporative crystallization, avoid adopting boiler, fire coal etc., reduce production costs, avoid the environmental pollution bringing thus simultaneously; By the setting of surface condenser 2, the indirect steam that crystallizing evaporator 3 is produced is condensed into distilled water, condensed distilled water contains micro-impurity, can not directly arrange outward, it can be delivered to condensed water storage tank 11 by being arranged on the condensating water outlet tube of surface condenser 2 bottoms, by condensate pump 12, use it for and dissolve Nacl or as sodium chlorate centrifuge washings etc., realize the recycling to industrial wastewater as required, reduce the pollution of industrial wastewater to environment.
The utility model operation principle: electrolyte is delivered in the evaporimeter in crystallizing evaporator 3 by interior circulation axial-flow pump 4 by feed pump 5, when the interior liquid level of crystallizing evaporator 3 reaches 40%, circulation axial-flow pump 4 in starting, under the effect of interior circulation axial-flow pump 4, chlorate/perchlorate solution in crystallizing evaporator 3 always in good circulation stirring state, then start vacuum unit 1, make crystallizing evaporator 3 vacuums reach preassigned.Thin brilliant liquid temp in crystallizing evaporator 3 is during lower than 50 ℃, start heat cycles pump 6, solution in crystallizer in crystallizing evaporator 3 as being delivered to, thin brilliant liquid is carried out to heat exchange in heat exchanger 7, and controlled circulation amount and temperature, keep looping like this, crystallizing evaporator 3 is always in normal running status, and indices is all in prescribed limit, while reaching predetermined operation, be positioned at material sedimentation chamber 13 magma liquid, by opening the outlet valve of crystallizing evaporator 3 discharging openings 14, and start discharging pump 8, discharging.The indirect steam that crystallizing evaporator 3 produces enters in surface condenser 2 and is condensed into distilled water, the heat of indirect steam is after surface condenser exchange, heat recirculated water being carried by cooling tower 9 is discharged into after atmosphere, the temperature of recirculated water reduces, by water circulating pump 10, return to surface condenser 2, continue to carry out heat exchange with the steam that just enters surface condenser 2 so constantly circulation.Distilled water in surface condenser 2, may contain trace impurity, be stored into as required condensed water storage tank 11, and export by condensate pump 12, for the washing of sodium chlorate centrifuge, dissolve Nacl or solid sodium chlorate etc., thereby avoided the waste of water resource, realize the recycling of industrial wastewater.
Embodiment 2:
The present embodiment further limits described crystallizing evaporator 3 cavity bottoms and is provided with material sedimentation chamber 13 on the basis of embodiment 1, material sedimentation chamber 13 is communicated with discharging pump 8 by being located at the discharging opening 14 of its chamber wall, in chlorate/perchlorate evaporating concentration process, form the crystallizing layer of different densities, the density that the closer to crystallizing evaporator 3 bottoms is material sedimentation chamber intercrystalline layer is larger, according to the requirement of chlorate/perchlorate evaporative crystallization product, the crystalline product that is positioned at material sedimentation chamber 13 is that magma liquid is by discharging opening 14, be delivered to discharging pump 8, enter centrifugal separation system.Other parts of the present embodiment are identical with embodiment 1, repeat no more.
Embodiment 3:
The present embodiment further limits described surface condenser 2 one end and is provided with circulating water outlet pipe on the basis of above-described embodiment, circulating water outlet pipe is connected with cooling tower 9, cooling tower 9 is connected with the circulating water intake pipe that is located at surface condenser 2 one end by water circulating pump 10, circulating water outlet pipe, circulating water intake Guan Jun is positioned at the same one end of surface condenser 2, the indirect steam that crystallizing evaporator 3 produces enters surface condenser 2 and is condensed into distilled water, the heat of distilled water condensation passes to the recirculated water in tubulation by the tubulation in surface condenser, recirculated water enters cooling tower 9 through circulating water outlet pipe, cooling tower 9 is provided with blower fan, the heat that recirculated water is carried is dispersed in atmosphere by cooling tower fan, recirculated water after cooling tower cooling enters surface condenser 2 by water circulating pump, continue condensation and from crystallizing evaporator 3, enter the steam of surface condenser, realizing recirculated water reuses, and the steam heat that crystallizing evaporator is produced is taken out of.Other parts of the present embodiment are same as the previously described embodiments, repeat no more.
Embodiment 4:
The present embodiment is on the basis of above-described embodiment, further limit described crystallizing evaporator 3 and comprise evaporimeter and crystallizer, crystallizer is positioned at evaporimeter lower end, crystallizer tube wall is provided with thin brilliant liquid outlet 15, described thin brilliant liquid outlet 15 is connected with heat cycles pump 6 by circulating line, the thin brilliant liquid producing through evaporation and concentration in crystallizer in crystallizing evaporator 3, by heat cycles pump 6, be delivered to heat exchanger 7, in heat exchanger 7, obtain heat, the heat energy that the cell reaction of origin of heat in chlorate/perchlorate electrolysis unit 16 produces, thin brilliant liquid enters interior circulation axial-flow pump 4 by circulating line, the evaporimeter thin brilliant liquid being delivered in crystallizing evaporator 3 by interior circulation axial-flow pump 4 is proceeded evaporation and concentration, thin brilliant liquid in obtaining the process of heat energy in heat exchanger 7, the heat producing with chlorate/perchlorate electrolysis unit 16 exchanges, the heat producing by the electrolysis of chlorate/perchlorate is as the external heat source of evaporative crystallization, thereby ban boiler investment, save coal, combustion gas, the fuel sources such as timber, the flue gas of avoiding boiler operatiopn to produce, scarp contaminated environment.Other parts of the present embodiment are same as the previously described embodiments, repeat no more.
Embodiment 5:
The present embodiment is on the basis of above-described embodiment, for preventing the corrosion of the materials such as chlorate/perchlorate to crystallizing evaporator 3, further limiting described crystallizing evaporator 3 materials is 316L stainless steel or dual phase steel stainless steel, in prior art, while adopting high temperature heat source, the preferred titanium material of material, but the use of titanium material has increased the equipment investment cost of crystallizing evaporator, and by the pressure of vacuum unit reduction crystallizing evaporator, and then the required heat energy of reduction solution evaporative crystallization, carry out at low temperatures evaporative crystallization, chlorate/perchlorate reduces the corrosivity of crystallizing evaporator, now, the preferred 316L of material or dual phase steel stainless steel, not only reduced the corrosivity to crystallizing evaporator, and equipment cost reduces greatly.Other structures of the present embodiment are same as the previously described embodiments, repeat no more.
Embodiment 6:
The present embodiment is on the basis of above-described embodiment, in order effectively to realize thin brilliant liquid, as heat transferring medium, in heat exchanger, carry out heat exchange, in heat exchanger 7, be provided with serpentine coil formula heat exchanger tube, the heat energy that in serpentine coil formula heat exchanger tube, sodium perchlorate electrolysis produces is as the external heat source of the heat transferring mediums such as thin brilliant liquid, and the thin brilliant liquid after heat exchange is proceeded condensing crystallizing by delivering in the evaporimeter in crystallizing evaporator 3 of interior circulation axial-flow pump 4.Other structures of the present embodiment are same as the previously described embodiments, repeat no more.
The above; it is only preferred embodiment of the present utility model; not the utility model is done to any pro forma restriction, any simple modification, equivalent variations that every foundation technical spirit of the present utility model is done above embodiment, all fall into protection domain of the present utility model.
Claims (7)
1. chlorate/perchlorate vacuum and low temperature evaporation and crystallization system, it is characterized in that: comprise the vacuum unit (1) connecting successively, surface condenser (2), crystallizing evaporator (3), interior circulation axial-flow pump (4) and feed pump (5), crystallizing evaporator (3) is connected with heating circulation system, heating circulation system comprises heat cycles pump (6) and the heat exchanger (7) connecting successively, heat exchanger (7) is connected with interior circulation axial-flow pump (4) by circulating line, heat exchanger (7) is also connected with chlorate/perchlorate electrolysis unit (16), surface condenser (2) bottom is provided with condensating water outlet tube, condensating water outlet tube successively with condensed water storage tank (11), condensate pump (12) connects.
2. a kind of chlorate/perchlorate vacuum and low temperature evaporation and crystallization system according to claim 1, it is characterized in that: described crystallizing evaporator (3) cavity bottom is provided with material sedimentation chamber (13), material sedimentation chamber (13) is communicated with discharging pump (8) by being located at the discharging opening (14) of its chamber wall.
3. a kind of chlorate/perchlorate vacuum and low temperature evaporation and crystallization system according to claim 1, it is characterized in that: described surface condenser (2) one end is provided with circulating water outlet pipe, circulating water outlet pipe is connected with cooling tower (9), cooling tower (9) is connected with the circulating water intake pipe that is located at surface condenser (2) one end by water circulating pump (10), and circulating water outlet pipe, circulating water intake Guan Jun are positioned at the same one end of surface condenser (2).
4. according to a kind of chlorate/perchlorate vacuum and low temperature evaporation and crystallization system described in claim 1 or 2 or 3, it is characterized in that: described crystallizing evaporator (3) comprises evaporimeter and crystallizer, crystallizer is positioned at evaporimeter lower end, and crystallizer tube wall is provided with thin brilliant liquid outlet (15).
5. a kind of chlorate/perchlorate vacuum and low temperature evaporation and crystallization system according to claim 4, is characterized in that: described thin brilliant liquid outlet (15) is connected with heat cycles pump (6) by circulating line.
6. a kind of chlorate/perchlorate vacuum and low temperature evaporation and crystallization system according to claim 5, is characterized in that: described crystallizing evaporator (3) material is 316L or dual phase steel stainless steel.
7. a kind of chlorate/perchlorate vacuum and low temperature evaporation and crystallization system according to claim 5, is characterized in that: described heat exchanger (7) is serpentine coil formula heat exchanger.
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| CN201420406393.1U CN203954705U (en) | 2014-07-23 | 2014-07-23 | A kind of chlorate/perchlorate vacuum and low temperature evaporation and crystallization system |
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| CN201420406393.1U CN203954705U (en) | 2014-07-23 | 2014-07-23 | A kind of chlorate/perchlorate vacuum and low temperature evaporation and crystallization system |
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| CN104478152A (en) * | 2014-12-29 | 2015-04-01 | 丹东东方机电工程有限公司 | Sodium-salt-containing waste water treatment device of desulfurization system |
| CN106379860A (en) * | 2016-08-30 | 2017-02-08 | 汝城县三鑫电化有限公司 | Potassium chlorate production equipment and method |
| CN110898450A (en) * | 2019-12-13 | 2020-03-24 | 石棉县天钰科技有限公司 | Device and method for potassium perchlorate mother liquor evaporation concentration process |
| CN110975314A (en) * | 2019-11-25 | 2020-04-10 | 湖南恒光科技股份有限公司 | Closed circulation process system and method for sodium chlorate crystallization and evaporation water |
| CN111494980A (en) * | 2020-04-20 | 2020-08-07 | 湖北东方化工有限公司 | System and method for nitrotoluene melt crystallization |
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2014
- 2014-07-23 CN CN201420406393.1U patent/CN203954705U/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104478152A (en) * | 2014-12-29 | 2015-04-01 | 丹东东方机电工程有限公司 | Sodium-salt-containing waste water treatment device of desulfurization system |
| CN104478152B (en) * | 2014-12-29 | 2016-04-27 | 丹东东方机电工程有限公司 | Desulphurization system is containing sodium salt wastewater treatment equipment |
| CN106379860A (en) * | 2016-08-30 | 2017-02-08 | 汝城县三鑫电化有限公司 | Potassium chlorate production equipment and method |
| CN110975314A (en) * | 2019-11-25 | 2020-04-10 | 湖南恒光科技股份有限公司 | Closed circulation process system and method for sodium chlorate crystallization and evaporation water |
| CN110898450A (en) * | 2019-12-13 | 2020-03-24 | 石棉县天钰科技有限公司 | Device and method for potassium perchlorate mother liquor evaporation concentration process |
| CN111494980A (en) * | 2020-04-20 | 2020-08-07 | 湖北东方化工有限公司 | System and method for nitrotoluene melt crystallization |
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