CN205099370U - High concentration contains salt waste water evaporation crystallization process device - Google Patents
High concentration contains salt waste water evaporation crystallization process device Download PDFInfo
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- CN205099370U CN205099370U CN201520914680.8U CN201520914680U CN205099370U CN 205099370 U CN205099370 U CN 205099370U CN 201520914680 U CN201520914680 U CN 201520914680U CN 205099370 U CN205099370 U CN 205099370U
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- pump
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- room
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- 239000002351 wastewater Substances 0.000 title claims abstract description 21
- 238000002425 crystallisation Methods 0.000 title claims abstract description 20
- 230000008025 crystallization Effects 0.000 title claims abstract description 19
- 150000003839 salts Chemical class 0.000 title claims abstract description 19
- 238000000034 method Methods 0.000 title abstract description 7
- 238000001704 evaporation Methods 0.000 title abstract description 5
- 230000008020 evaporation Effects 0.000 title abstract description 3
- 239000012452 mother liquor Substances 0.000 claims abstract description 50
- 238000010438 heat treatment Methods 0.000 claims abstract description 43
- 239000002002 slurry Substances 0.000 claims abstract description 31
- 238000003860 storage Methods 0.000 claims abstract description 22
- 239000002994 raw material Substances 0.000 claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- 238000009833 condensation Methods 0.000 claims description 22
- 230000005494 condensation Effects 0.000 claims description 22
- 210000002966 serum Anatomy 0.000 claims description 16
- 239000012530 fluid Substances 0.000 claims description 11
- 230000008676 import Effects 0.000 claims description 4
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 abstract description 36
- 239000007788 liquid Substances 0.000 abstract description 18
- 239000010413 mother solution Substances 0.000 abstract description 3
- 239000013078 crystal Substances 0.000 description 24
- 239000011780 sodium chloride Substances 0.000 description 17
- 239000000243 solution Substances 0.000 description 11
- DPDMMXDBJGCCQC-UHFFFAOYSA-N [Na].[Cl] Chemical compound [Na].[Cl] DPDMMXDBJGCCQC-UHFFFAOYSA-N 0.000 description 8
- 239000002245 particle Substances 0.000 description 8
- 239000006228 supernatant Substances 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 235000013339 cereals Nutrition 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 230000000903 blocking effect Effects 0.000 description 3
- 239000010419 fine particle Substances 0.000 description 3
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 239000005046 Chlorosilane Substances 0.000 description 1
- 206010039509 Scab Diseases 0.000 description 1
- BLRPTPMANUNPDV-UHFFFAOYSA-N Silane Chemical compound [SiH4] BLRPTPMANUNPDV-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- KOPOQZFJUQMUML-UHFFFAOYSA-N chlorosilane Chemical compound Cl[SiH3] KOPOQZFJUQMUML-UHFFFAOYSA-N 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 235000013312 flour Nutrition 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005498 polishing Methods 0.000 description 1
- 229910021420 polycrystalline silicon Inorganic materials 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910000077 silane Inorganic materials 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000009997 thermal pre-treatment Methods 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model provides a high concentration contains salt waste water evaporation crystallization process device, includes raw materials storage tank, charge pump, plate heat exchanger, circulating pump, heating chamber, evaporated crystallizer, thick liquid pump, hydraulic cyclone, slurry bucket, doublestage pushing centrifugal machine, vibrations fluidized bed dryer, mother solution storage tank, mother liquor pump, its characterized in that: charge pump, plate heat exchanger, circulating pump, heating chamber, evaporated crystallizer, thick liquid pump, hydraulic cyclone, slurry bucket, doublestage pushing centrifugal machine, vibrations fluidized bed dryer, mother solution storage tank, mother liquor pump are connected in proper order to the raw materials storage tank, plate heat exchanger upper portion is equipped with the export of plate heat exchanger thick liquid, and the export of plate heat exchanger thick liquid is connected with the circulating pump through the pipeline, circulating pump export and heating chamber mother liquor access connection. The utility model discloses the naCl quality that finally obtains reaches the purified salt secondary standard requirement that (GBT5462 -2003) national industry salt standard required, promptly naCl >= 97.5%.
Description
Technical field
The utility model relates to a kind of evaporated crystallization device, especially relates to a kind of high-concentration salt-containing wastewater evaporative crystallization treatment unit.
Background technology
At present, crystallisation by cooling discontinuous crystallization processes account for more than 95% in every profession and trade at home, and labour productivity is low, mainly manual operation, quality product can not be guaranteed, and comprehensive energy consumption is high, and corrodibility is large, plugging, the phenomenon that scabs are given prominence to, need often cleaning, labour intensity large user do not welcome, more importantly product granularity thin (have as flour), dehydration difficulty, caking has had a strong impact on the quality of product.
Summary of the invention
The utility model is for the problems referred to above, there is provided a kind of high-concentration salt-containing wastewater evaporative crystallization treatment unit, after sodium chloride waste water heating, concentrated solution reaches supersaturation, comes downwards to bottom crystal grain graded region through central circulating tube, then upwards flow and crystallize out, the crystal grain of separating out floats and flows in liquid stream upwards, and with liquid upwards, macrobead is downward for little crystal grain, like this, in crystal grain graded region, crystal grain is increasing from top to bottom, forms classification.Modified hot solution the flow of evaporative crystallizer can be flowed back to by regulating the rate of discharge of recycle pump, thus the speed that change liquid upwards flows bottom central circulating tube, and then change the upper and lower crystal grain size of crystal grain graded region, the top of educating brilliant room is supernatant liquor, supernatant liquor is transported to after oven heats through mother liquor outlet and enters evaporator room slurry inlet again, because supernatant liquor contains very fine particle, in heat-processed, non flouling behaviour and blocking heating tube pipeline, enable evaporative process carry out continuously; The NaCl quality finally obtained reaches the purified salt secondary standard requirement of (GBT5462-2003) National Industrial salt standard-required, i.e. NaCl >=97.5%, granularity >=0.8mm, uniform particles, any surface finish; This device comprehensive energy consumption is low; Not plugging, non-scaling, grain size number is large, smooth appearance.
The technical solution of the utility model is: a kind of high-concentration salt-containing wastewater evaporative crystallization treatment unit, comprises raw material storage tank, fresh feed pump, plate-type heat exchanger, recycle pump, heating chamber, evaporative crystallizer, slush pump, hydrocyclone, slurries bucket, two-stage material-pushing centrifuge, vibrations fluid bed dryer, mother liquor holding tank, mother liquor pump, is characterized in that: described raw material storage tank is linked in sequence fresh feed pump, plate-type heat exchanger, recycle pump, heating chamber, evaporative crystallizer, slush pump, hydrocyclone, slurries bucket, two-stage material-pushing centrifuge, vibrations fluid bed dryer, mother liquor holding tank, mother liquor pump, described plate-type heat exchanger top is provided with plate-type heat exchanger serum outlet, and plate-type heat exchanger serum outlet is connected with recycle pump by pipeline, and circulating-pump outlet is connected with the import of heating chamber mother liquor, and evaporative crystallizer comprises evaporator room, central circulating tube, educate brilliant room, evaporator room is connected to the top of central circulating tube, central circulating tube stretches into educates brilliant indoor, evaporator room is provided with top secondary steam outlet and bottom evaporator room slurry inlet, educate brilliant room and be provided with top mother liquor outlet and Yu Jing room, bottom serum outlet, the evaporator room slurry inlet of evaporator room is in the same side with the mother liquor outlet of educating brilliant room, the outlet of central circulating tube is positioned at the below of mother liquor outlet, evaporator room and educate between brilliant room and be communicated with vapour phase pipe, educate brilliant room to have and the shoulder be connected bottom evaporator room, one end of vapour phase pipe is installed on shoulder, the other end of vapour phase pipe is installed in the evaporator room slurry inlet opposing sidewalls of evaporator room, educate brilliant room serum outlet to be connected with slush pump by pipeline, slush pump is connected with hydrocyclone by pipeline, hydrocyclone is arranged on slurries bucket top, slurries bucket is connected with two-stage material-pushing centrifuge by pipeline, two-stage material-pushing centrifuge lead up to pipeline with vibrations fluid bed dryer be connected, two-stage material-pushing centrifuge is separately leaded up to pipeline and is connected with mother liquor holding tank, mother liquor holding tank is connected with mother liquor pump by pipeline, mother liquor pump is connected with recycle pump by pipeline, heating chamber top is connected with evaporator room slurry inlet by pipeline, heating chamber top is provided with steam-in, steam-in is connected with steam storage tank by pipeline, heating chamber bottom is provided with heating chamber vapor condensation water out, heating chamber vapor condensation water out is connected with condensed water bucket by pipeline, condensed water bucket is connected with vapor condensation water pump by pipeline, vapor condensation water pump is connected with plate-type heat exchanger condensing water inlet by pipeline, plate-type heat exchanger condensation-water drain is connected with water of condensation storage tank by pipeline.
The beneficial effects of the utility model are:
1, comprehensive energy consumption is low:
Adopt this evaporated crystallization device, make full use of the heat of water of condensation to reduce the energy consumption of system, to evaporate sodium chloride-containing waste water 19t/h (concentration of polymer solution 8.464%) for calculating, namely 4.25T/h steam is needed, 1 ton of steam raising sodium chloride-containing waste water 4.47 tons, energy consumption is low, reaches energy-conservation object.
2, the quality of sodium-chlor is high:
By this evaporated crystallization device by the waste water evaporative crystallization containing sodium-chlor and other foreign ion, the NaCl quality finally obtained reaches the purified salt secondary standard requirement of (GBT5462-2003) National Industrial salt standard-required, i.e. NaCl >=97.5%.
3, not plugging, non-scaling:
Plugging is because single tube superheating temperature raises in vacuum evaporating crystalization device, to come to life evaporation at heating tube upper orifice, the nucleus of sodium-chlor starts crystallization, the sodium-chlor that crystallization generates is adsorbed on the mouth of pipe of upcast, sometimes hundreds of heating tubes can block up 1/3 even 1/2, decrease heat interchanging area and have had a strong impact on the steam output of sodium chloride-containing waste water.This device, by reducing single tube superheating temperature, optimizes the length-to-diameter ratio of heating tube, optimizes the parameters such as the above waste water liquid level of tube sheet, solves plugging problem;
Fouling is evaporated because saturated solution boiling is splashed on tank skin, and form very thick sodium-chlor dirt, its knot is meeting self falling after certain thickness, the recycle pump of vaporizer, thermometer, pressure unit etc. is smashed, can cause stopping production time serious.This device, by increasing the measure of polishing tank skin, adds the measure of coil pipe spray tank skin, this phenomenon of fouling is eliminated above tank skin.
4, grain size number is large, smooth appearance:
Have in this evaporative crystallizer and educate brilliant room compared with large regions, educate in brilliant room and the nucleus of sodium-chlor can be separated with mother liquor, effectively ensure that the quality of sodium-chlor, to ensure in Recycling Mother Solution without nucleus thus to ensure the quality of product, make grain size number can at more than 0.8mm, and uniform particles any surface finish.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
In Fig. 1, 1. raw material storage tank, 2. fresh feed pump, 3. plate-type heat exchanger, 4. recycle pump, 5. heating chamber, 6. evaporative crystallizer, 7. slush pump, 8. hydrocyclone, 9. slurries bucket, 10. two-stage material-pushing centrifuge, 11. vibrations fluid bed dryers, 12. mother liquor holding tanks, 13. mother liquor pumps, 14. vapor condensation water pumps, 15. plate-type heat exchanger condensation-water drains, 16. water of condensation storage tanks, 17. plate-type heat exchanger condensing water inlets, 18. plate-type heat exchanger serum outlet, 19. condensed water buckets, 20. heating chamber vapor condensation water outs, 21. steam storage tanks, 22. steam-ins, 23. secondary steam outlets, 24. evaporator rooms, 25. vapour phase pipes, 26. shoulders, 27. central circulating tubes, 28. educate brilliant room, 29. educate brilliant room serum outlet, 30. evaporator room slurry inlet, 31. mother liquor outlet, 32. heating chamber mother liquor imports.
Embodiment
Below in conjunction with accompanying drawing, the utility model is further described.
As shown in Figure 1, the utility model is a kind of high-concentration salt-containing wastewater evaporative crystallization treatment unit, comprise raw material storage tank 1, fresh feed pump 2, plate-type heat exchanger 3, recycle pump 4, heating chamber 5, evaporative crystallizer 6, slush pump 7, hydrocyclone 8, slurries bucket 9, two-stage material-pushing centrifuge 10, vibrations fluid bed dryer 11, mother liquor holding tank 12, mother liquor pump 13, it is characterized in that: described raw material storage tank 1 is linked in sequence fresh feed pump 2, plate-type heat exchanger 3, recycle pump 4, heating chamber 5, evaporative crystallizer 6, slush pump 7, hydrocyclone 8, slurries bucket 9, two-stage material-pushing centrifuge 10, vibrations fluid bed dryer 11, mother liquor holding tank 12, mother liquor pump 13, described plate-type heat exchanger 3 top is provided with plate-type heat exchanger serum outlet 18, plate-type heat exchanger serum outlet 18 is connected with recycle pump 4 by pipeline, recycle pump 4 outlet is connected with heating chamber mother liquor import 32, evaporative crystallizer 6 comprises evaporator room 24, central circulating tube 27, educate brilliant room 28, evaporator room 24 is connected to the top of central circulating tube 27, central circulating tube 27 stretches into educates in brilliant room 28, evaporator room 24 is provided with top secondary steam outlet 23 and bottom evaporator room slurry inlet 30, educate brilliant room 28 and be provided with top mother liquor outlet 31 and Yu Jing room, bottom serum outlet 29, the evaporator room slurry inlet 30 of evaporator room 24 is in the same side with the mother liquor outlet 31 of educating brilliant room 28, the outlet of central circulating tube 27 is positioned at the below of mother liquor outlet 31, evaporator room 24 and educate between brilliant room 28 and be communicated with vapour phase pipe 25, educate brilliant room 28 to have and the shoulder 26 be connected bottom evaporator room 24, one end of vapour phase pipe 25 is installed on shoulder 26, the other end of vapour phase pipe 25 is installed in evaporator room slurry inlet 30 opposing sidewalls of evaporator room 24, educate brilliant room serum outlet 29 to be connected with slush pump 7 by pipeline, slush pump 7 is connected with hydrocyclone 8 by pipeline, hydrocyclone 8 is arranged on slurries bucket 9 top, slurries bucket 9 is connected with two-stage material-pushing centrifuge 10 by pipeline, two-stage material-pushing centrifuge 10 lead up to pipeline with vibrations fluid bed dryer 11 be connected, two-stage material-pushing centrifuge 10 is separately leaded up to pipeline and is connected with mother liquor holding tank 12, mother liquor holding tank 12 is connected with mother liquor pump 13 by pipeline, mother liquor pump 13 is connected with recycle pump 4 by pipeline, heating chamber 5 top is connected with evaporator room slurry inlet 30 by pipeline, heating chamber 5 top is provided with steam-in 22, steam-in 22 is connected with steam storage tank 21 by pipeline, heating chamber 5 bottom is provided with heating chamber vapor condensation water out 20, heating chamber vapor condensation water out 20 is connected with condensed water bucket 19 by pipeline, condensed water bucket 19 is connected with vapor condensation water pump 14 by pipeline, vapor condensation water pump 14 is connected with plate-type heat exchanger condensing water inlet 17 by pipeline, plate-type heat exchanger condensation-water drain 15 is connected with water of condensation storage tank 16 by pipeline.
Working process of the present utility model is: sodium chloride-containing waste water (the flow 19t/h generated after the polycrystalline silicon device chlorine-containing silane waste gas in raw material storage tank 1 and chlorosilane raffinate carrying out washing treatment, sodium chloride solution mass concentration 8.464%, original liquid temperature 25 DEG C), plate-type heat exchanger 3 is entered under fresh feed pump 2 acts on, carry out thermal pretreatment, the temperature of preheating post chlorization sodium waste water is 50 DEG C, pressure 0.28MPa, then heating chamber 5 is entered, from the 0.7MPa of steam storage tank 21, the saturation steam of 170 DEG C, enters heating chamber 5, heats sodium chloride waste water;
Heating post chlorization sodium waste water became hot solution (temperature 98 DEG C, pressure 0.07MPa), then enter evaporative crystallizer 6 evaporative crystallization, concentrated solution reaches supersaturation, come downwards to bottom crystal grain graded region through central circulating tube 27, then upwards flow and crystallize out.The crystal grain of separating out floats and flows in liquid stream upwards, and with liquid upwards, macrobead is downward, and like this, in crystal grain graded region, crystal grain is increasing from top to bottom for little crystal grain, forms classification.By regulating the rate of discharge of recycle pump 4 modified hot solution can flow back to the flow of evaporative crystallizer 6, thus change the speed that liquid upwards flows bottom central circulating tube 27, and then change the upper and lower crystal grain size of crystal grain graded region.Such as, the overheated solution flow flowing back to evaporative crystallizer 6 is larger, and crystal grain graded region flow stream velocity is upwards faster, and the particle taken away by the liquid stream upwards flowed is larger, and bottom particles is larger, and the crystal product particle obtained is larger.Otherwise less, use this means, the size of crystalline product particle can be regulated, realize sodium chloride waste water continuous print evaporative crystallization, because supernatant liquor contains very fine particle, in heat-processed, non flouling behaviour and blocking heating tube pipeline, enable evaporative process carry out continuously.Be deposited to the crystal of educating bottom brilliant room 28 and send into hydrocyclone 8 from educating brilliant room serum outlet 29 by slush pump 7, under the effect of hydrocyclone 8, underflow liquid exports from hydrocyclone 8 and flows out, enter slurries bucket 9, then enter two-stage material-pushing centrifuge 10 and carry out solid-liquid separation, sodium-chlor xln flows out from two-stage material-pushing centrifuge 10, enter vibrations fluid bed dryer 11 and carry out drying treatment, NaCl (1500Kg/h) quality obtained reaches the purified salt secondary standard requirement of (GBT5462-2003) National Industrial salt standard-required, i.e. NaCl >=97.5%, granularity >=0.8mm, uniform particles, any surface finish, mother liquor flows into mother liquor holding tank 12 from whizzer 10 serum outlet, and mother liquor is sent into heating chamber 5 through mother liquor pump 13 and carried out circulating and evaporating crystallization,
Enter condensed water bucket 19 from heating chamber 5 steam condensate (temperature is 90 DEG C, pressure 0.15MPa) out, enter plate-type heat exchanger 3 by vapor condensation water pump 14; After heat exchange, (temperature is 48 DEG C, pressure 0.08MPa) enters water of condensation storage tank 16, and water of condensation obtains reuse, energy efficient, reaches energy-conservation object.
As can be seen here, the utility model provides a kind of high-concentration salt-containing wastewater evaporative crystallization treatment unit, and after sodium chloride waste water heating, concentrated solution reaches supersaturation, comes downwards to bottom crystal grain graded region through central circulating tube, then upwards flow and crystallize out, the crystal grain of separating out floats and flows in liquid stream upwards, and with liquid upwards, macrobead is downward for little crystal grain, like this, in crystal grain graded region, crystal grain is increasing from top to bottom, forms classification.Modified hot solution the flow of evaporative crystallizer can be flowed back to by regulating the rate of discharge of recycle pump, thus the speed that change liquid upwards flows bottom central circulating tube, and then change the upper and lower crystal grain size of crystal grain graded region, the top of educating brilliant room is supernatant liquor, supernatant liquor is transported to after oven heats through mother liquor outlet and enters evaporator room slurry inlet again, because supernatant liquor contains very fine particle, in heat-processed, non flouling behaviour and blocking heating tube pipeline, enable evaporative process carry out continuously; The NaCl quality finally obtained reaches the purified salt secondary standard requirement of (GBT5462-2003) National Industrial salt standard-required, i.e. NaCl >=97.5%, granularity >=0.8mm, uniform particles, any surface finish; This device comprehensive energy consumption is low; Not plugging, non-scaling, grain size number is large, smooth appearance.
Claims (1)
1. a high-concentration salt-containing wastewater evaporative crystallization treatment unit, comprises raw material storage tank, fresh feed pump, plate-type heat exchanger, recycle pump, heating chamber, evaporative crystallizer, slush pump, hydrocyclone, slurries bucket, two-stage material-pushing centrifuge, vibrations fluid bed dryer, mother liquor holding tank, mother liquor pump, is characterized in that: described raw material storage tank is linked in sequence fresh feed pump, plate-type heat exchanger, recycle pump, heating chamber, evaporative crystallizer, slush pump, hydrocyclone, slurries bucket, two-stage material-pushing centrifuge, vibrations fluid bed dryer, mother liquor holding tank, mother liquor pump, described plate-type heat exchanger top is provided with plate-type heat exchanger serum outlet, and plate-type heat exchanger serum outlet is connected with recycle pump by pipeline, and circulating-pump outlet is connected with the import of heating chamber mother liquor, and evaporative crystallizer comprises evaporator room, central circulating tube, educate brilliant room, evaporator room is connected to the top of central circulating tube, central circulating tube stretches into educates brilliant indoor, evaporator room is provided with top secondary steam outlet and bottom evaporator room slurry inlet, educate brilliant room and be provided with top mother liquor outlet and Yu Jing room, bottom serum outlet, the evaporator room slurry inlet of evaporator room is in the same side with the mother liquor outlet of educating brilliant room, the outlet of central circulating tube is positioned at the below of mother liquor outlet, evaporator room and educate between brilliant room and be communicated with vapour phase pipe, educate brilliant room to have and the shoulder be connected bottom evaporator room, one end of vapour phase pipe is installed on shoulder, the other end of vapour phase pipe is installed in the evaporator room slurry inlet opposing sidewalls of evaporator room, educate brilliant room serum outlet to be connected with slush pump by pipeline, slush pump is connected with hydrocyclone by pipeline, hydrocyclone is arranged on slurries bucket top, slurries bucket is connected with two-stage material-pushing centrifuge by pipeline, two-stage material-pushing centrifuge lead up to pipeline with vibrations fluid bed dryer be connected, two-stage material-pushing centrifuge is separately leaded up to pipeline and is connected with mother liquor holding tank, mother liquor holding tank is connected with mother liquor pump by pipeline, mother liquor pump is connected with recycle pump by pipeline, heating chamber top is connected with evaporator room slurry inlet by pipeline, heating chamber top is provided with steam-in, steam-in is connected with steam storage tank by pipeline, heating chamber bottom is provided with heating chamber vapor condensation water out, heating chamber vapor condensation water out is connected with condensed water bucket by pipeline, condensed water bucket is connected with vapor condensation water pump by pipeline, vapor condensation water pump is connected with plate-type heat exchanger condensing water inlet by pipeline, plate-type heat exchanger condensation-water drain is connected with water of condensation storage tank by pipeline.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520914680.8U CN205099370U (en) | 2015-11-08 | 2015-11-08 | High concentration contains salt waste water evaporation crystallization process device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520914680.8U CN205099370U (en) | 2015-11-08 | 2015-11-08 | High concentration contains salt waste water evaporation crystallization process device |
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| Publication Number | Publication Date |
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| CN205099370U true CN205099370U (en) | 2016-03-23 |
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| CN201520914680.8U Expired - Fee Related CN205099370U (en) | 2015-11-08 | 2015-11-08 | High concentration contains salt waste water evaporation crystallization process device |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109289234A (en) * | 2018-10-31 | 2019-02-01 | 浙江新和成股份有限公司 | For the device of evaporative crystallization, the method for crystallising of vitamin B6 |
| CN110723857A (en) * | 2019-11-21 | 2020-01-24 | 东莞市三人行环境科技有限公司 | High-salinity water concentration and crystallization treatment system and process |
| WO2020233392A1 (en) * | 2019-05-20 | 2020-11-26 | 江苏嘉泰蒸发设备股份有限公司 | Evaporation crystallization device for brine waste containing large amount of organic matters and tar |
| CN113184933A (en) * | 2021-04-27 | 2021-07-30 | 国家能源集团宁夏煤业有限责任公司 | Evaporative crystallization system |
| CN115025513A (en) * | 2022-07-07 | 2022-09-09 | 科立鑫(珠海)新能源有限公司 | Continuous crystallization process and equipment for coarse-particle cobalt sulfate |
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2015
- 2015-11-08 CN CN201520914680.8U patent/CN205099370U/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109289234A (en) * | 2018-10-31 | 2019-02-01 | 浙江新和成股份有限公司 | For the device of evaporative crystallization, the method for crystallising of vitamin B6 |
| CN109289234B (en) * | 2018-10-31 | 2020-12-15 | 浙江新和成股份有限公司 | Device for evaporative crystallization and crystallization method of vitamin B6 |
| WO2020233392A1 (en) * | 2019-05-20 | 2020-11-26 | 江苏嘉泰蒸发设备股份有限公司 | Evaporation crystallization device for brine waste containing large amount of organic matters and tar |
| CN110723857A (en) * | 2019-11-21 | 2020-01-24 | 东莞市三人行环境科技有限公司 | High-salinity water concentration and crystallization treatment system and process |
| CN113184933A (en) * | 2021-04-27 | 2021-07-30 | 国家能源集团宁夏煤业有限责任公司 | Evaporative crystallization system |
| CN115025513A (en) * | 2022-07-07 | 2022-09-09 | 科立鑫(珠海)新能源有限公司 | Continuous crystallization process and equipment for coarse-particle cobalt sulfate |
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