CN205099538U - High concentration contains salt waste water MVR evaporation crystallization process system - Google Patents
High concentration contains salt waste water MVR evaporation crystallization process system Download PDFInfo
- Publication number
- CN205099538U CN205099538U CN201520873716.2U CN201520873716U CN205099538U CN 205099538 U CN205099538 U CN 205099538U CN 201520873716 U CN201520873716 U CN 201520873716U CN 205099538 U CN205099538 U CN 205099538U
- Authority
- CN
- China
- Prior art keywords
- pipeline
- crystallizer
- mother liquor
- pump
- outlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
Abstract
High concentration contains salt waste water MVR evaporation crystallization process system, including raw materials storage tank, charge pump, plate heat exchanger, DTB evaporated crystallizer heating chamber, DTB evaporated crystallizer, vacuum evaporated crystallizer heating chamber, vacuum evaporated crystallizer, hydraulic cyclone, sodium sulphate slurry bucket, doublestage pushing centrifugal machine, vibrations fluidized bed dryer, mother solution storage tank, mother liquor pump, evaporated crystallizer 0 pump, its evaporated crystallizer 1: charge pump, plate heat exchanger, DTB evaporated crystallizer heating chamber, DTB evaporated crystallizer, vacuum evaporated crystallizer heating chamber are connected in proper order to the raw materials storage tank. The utility model discloses the comprehensive energy consumption is low, and the anhydrous sodium sulphate quality that finally obtains reaches the requirement of GBT6009 -2014 " industry anhydrous sodium sulphate " II class acceptable end product, and sodium sulphate content >= 98% wherein, industry sodium chloride reach exposure to sunlight sodium chloride secondary standard requirement in the national industry sodium chloride standard (GBT5462 -2003).
Description
Technical field
The utility model relates to a kind of evaporation and crystallization system, especially relates to high-concentration salt-containing wastewater MVR evaporative crystallization treatment system.
Background technology
The output about 3,000 ten thousand tons in China well mine salt saltcake type ore deposit, accounts for 50% of national salt output.Whole nation saltcake type salt mine is distributed in the provinces such as Hubei, Hunan, Jiangxi, Yunnan, Anhui, Jiangsu, Shandong, Shaanxi.Most based on vacuum salt, the throughput of single complete equipment 60 ~ 1,000,000 tons/year.The equipment adopted mainly contains falling film evaporation crystallizer, FC type evaporative crystallizer, Oslo evaporative crystallizer etc.; But when processing high-concentration salt-containing wastewater, there is following defect in these equipment:
1, falling film evaporation crystallizer, very easily cause dry wall fouling, need often clean, labour intensity large user do not welcome;
2, FC type evaporative crystallizer, crystal size is little, greatly about 0.15-0.3mm, dehydration difficulty, caking has a strong impact on the quality of product, heating tube not easy cleaning and tube wall easy to wear;
3, Oslo evaporative crystallizer, complex structure, volume is large, and energy consumption is high, and corrodibility is large, and plugging, the phenomenon that scabs are given prominence to.
Summary of the invention
The utility model is for the problems referred to above, high-concentration salt-containing wastewater MVR evaporative crystallization treatment system is provided, this system is disposable before DTB evaporative crystallizer starts passes into saturation steam, after treating feed liquid boiling, secondary steam adopts MVR vapour compressor to carry out compression cycle utilization, do not re-use saturation steam, energy efficient, reach energy-conservation object, will containing sodium sulfate by MVR evaporation and crystallization system, the waste water evaporative crystallization of sodium-chlor and other foreign ion, sodium sulfate and sodium-chlor are separated, the anhydrous sodium sulphate quality finally obtained reaches the requirement of GB/T6009-2014 " industrial anhydrous sodium sulfate " II class acceptable end product, wherein sodium sulphate content >=98%, industrial chlorinations sodium reaches Exposure to Sunlight sodium-chlor secondary standard requirement in National Industrial sodium-chlor standard (GBT5462-2003), all the other heavy metals and other metal ions by mother liquor regularly or continuous print form of export be disposed to prime pretreatment system.System synthesis energy consumption is low; Not plugging, non-scaling, grain size number is large, smooth appearance.
The technical solution of the utility model is: high-concentration salt-containing wastewater MVR evaporative crystallization treatment system, comprise raw material storage tank, fresh feed pump, plate-type heat exchanger, DTB evaporative crystallizer heating chamber, DTB evaporative crystallizer, vacuum evaporation crystallizer heating chamber, vacuum evaporation crystallizer, a hydrocyclone, sodium sulfate slurries bucket, two-stage material-pushing centrifuge, vibrations fluid bed dryer, a mother liquor holding tank, a mother liquor pump, Recycling Mother Solution pump, it is characterized in that: described raw material storage tank is linked in sequence fresh feed pump, plate-type heat exchanger, DTB evaporative crystallizer heating chamber, DTB evaporative crystallizer, vacuum evaporation crystallizer heating chamber, vacuum evaporation crystallizer, a hydrocyclone, sodium sulfate slurries bucket, two-stage material-pushing centrifuge, vibrations fluid bed dryer, a mother liquor holding tank, a mother liquor pump, Recycling Mother Solution pump, described plate-type heat exchanger top is provided with plate-type heat exchanger serum outlet, plate-type heat exchanger serum outlet is connected with the import of DTB evaporative crystallizer lower slurry by pipeline, DTB evaporative crystallizer vertical-type axial-flow pump is installed bottom DTB evaporative crystallizer, it is DTB evaporative crystallizer mother liquor room in the middle part of DTB evaporative crystallizer, side, DTB evaporative crystallizer mother liquor room is provided with mother liquor outlet, mother liquor outlet is connected with DTB evaporative crystallizer recycle pump by pipeline, DTB evaporative crystallizer circulating-pump outlet is connected with the import of heating chamber lower slurry by pipeline, the outlet of heating chamber lower slurry is connected with the import of DTB evaporative crystallizer lower slurry by pipeline, DTB evaporative crystallizer mother liquor room opposite side is provided with mother liquor outlet, mother liquor outlet is connected with the import of vacuum evaporation crystallizer lower slurry by pipeline, the outlet of DTB evaporative crystallizer lower slurry is connected with sodium sulfate slush pump by pipeline, sodium sulfate slush pump is connected with a hydrocyclone by pipeline, a hydrocyclone is arranged on sodium sulfate slurries bucket top, sodium sulfate 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 a mother liquor holding tank, a mother liquor holding tank is connected with a mother liquor pump by pipeline, a mother liquor pump is connected with Recycling Mother Solution pump by pipeline, Recycling Mother Solution pump is connected with the import of DTB evaporative crystallizer lower slurry by pipeline one tunnel, another road is connected with mother liquor discharge outlet, vacuum evaporation crystallizer vertical-type axial-flow pump is installed bottom vacuum evaporation crystallizer, it is vacuum evaporation crystallizer mother liquor room in the middle part of vacuum evaporation crystallizer, side, vacuum evaporation crystallizer mother liquor room is provided with mother liquor outlet, mother liquor outlet is connected with vacuum evaporation crystallizer recycle pump by pipeline, vacuum evaporation crystallizer circulating-pump outlet is connected with the import of heating chamber lower slurry by pipeline, the outlet of heating chamber lower slurry is connected with the import of vacuum evaporation crystallizer lower slurry by pipeline, vacuum evaporation crystallizer mother liquor room opposite side is provided with mother liquor outlet, mother liquor outlet is connected with Recycling Mother Solution pump by pipeline, the outlet of vacuum evaporation crystallizer lower slurry is connected with sodium-chlor slush pump by pipeline, sodium-chlor slush pump is connected with No. two hydrocyclones by pipeline, No. two hydrocyclones are arranged on sodium-chlor slurries bucket top, sodium-chlor slurries bucket is connected with horizontal spiral centrifuge by pipeline, horizontal spiral centrifuge is connected with No. two mother liquor holding tanks by pipeline, No. two mother liquor holding tanks are connected with No. two mother liquor pumps by pipeline, No. two mother liquor pumps are connected with the import of vacuum evaporation crystallizer lower slurry by pipeline, DTB evaporative crystallizer heating chamber top is provided with steam-in, steam-in is connected with steam storage tank by pipeline, vacuum evaporation crystallizer heating chamber top is provided with steam-in, steam-in is connected with steam storage tank by pipeline, DTB evaporative crystallizer top is provided with secondary steam outlet, secondary steam outlet is connected with MVR vapour compressor by pipeline, MVR vapour compressor is provided with steam-in by pipeline with DTB evaporative crystallizer heating chamber top and is connected, vacuum evaporation crystallizer top is provided with secondary steam outlet, secondary steam outlet is connected with surface cooler by pipeline, surface cooler is connected with water ring vacuum pump by pipeline, water ring vacuum pump is connected with steam separator by pipeline, side, surface cooler bottom is provided with entrance of cooling water, opposite side is provided with cooling water outlet, entrance of cooling water is connected with cooling water tank by pipeline, cooling water outlet is connected with water coolant reuse tank by pipeline, be connected with condensation water tank by pipeline bottom surface cooler, condensation water tank is connected with condensate pump by pipeline, condensate pump is connected with water of condensation storage tank by pipeline, water of condensation storage tank is connected with recycling condensing water pump by pipeline, recycling condensing water pump is connected with DTB evaporative crystallizer wire mesh demister rinse mouth by pipeline one tunnel, recycling condensing water pump is connected with vacuum evaporation crystallizer wire mesh demister rinse mouth by another road of pipeline, heating chamber vapor condensation water out is provided with in the middle part of DTB evaporative crystallizer heating chamber, 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, heating chamber vapor condensation water out is provided with in the middle part of vacuum evaporation crystallizer heating chamber, 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 MVR mechanical recompression evaporation and crystallization system, disposablely before evaporative crystallizer starts pass into saturation steam, after treating feed liquid boiling, secondary steam employing MVR vapour compressor carries out compression cycle utilization, does not re-use saturation steam, energy efficient;
2, the quality of sodium sulfate, sodium-chlor is high:
By MVR evaporation and crystallization system by the waste water evaporative crystallization containing sodium sulfate, sodium-chlor and other foreign ion, sodium sulfate and sodium-chlor are separated, the anhydrous sodium sulphate quality finally obtained reaches the requirement of GB/T6009-2014 " industrial anhydrous sodium sulfate " II class acceptable end product, wherein sodium sulphate content >=98%, industrial chlorinations sodium reaches Exposure to Sunlight sodium-chlor secondary standard requirement in National Industrial sodium-chlor standard (GBT5462-2003), all the other heavy metals and other metal ions by mother liquor regularly or continuous print form of export be disposed to prime pretreatment system.
3, not plugging, non-scaling:
Plugging is because single tube superheating temperature raises in vacuum evaporating crystalization system, to come to life evaporation at heating tube upper orifice, the nucleus of sodium sulfate, sodium-chlor starts crystallization, the sodium sulfate that crystallization generates, sodium-chlor are 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 contains sodium sulfate, sodium chloride waste water.Native system, 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.Native system, 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:
Adopt DTB type evaporative crystallizer, vacuum evaporation crystallizer, because DTB type crystallizer, the mother liquor room compared with large regions is had in vacuum evaporation crystallizer, the nucleus of sodium-chlor or sodium sulfate can be separated with mother liquor in mother liquor room, the sodium-chlor contained in the mother liquor of supernatant liquor or metabisulfite solution are disposed to sodium-chlor or sulfate crystal system by the form that mother liquor discharges, effectively ensure that the quality of sodium sulfate, also ensure that the quality of sodium-chlor simultaneously, 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.DTB evaporative crystallizer heating chamber, 5.DTB evaporative crystallizer, 6. vacuum evaporation crystallizer heating chamber, 7. vacuum evaporation crystallizer, 8. a hydrocyclone, 9. sodium sulfate slurries bucket, 10. two-stage material-pushing centrifuge, 11. vibrations fluid bed dryers, No. 12. mother liquor holding tanks, No. 13. mother liquor pumps, 14. Recycling Mother Solution pumps, 15. plate-type heat exchanger serum outlet, the import of 16.DTB evaporative crystallizer lower slurry, 17. mother liquor outlet, 18.DTB evaporative crystallizer recycle pump, 19. heating chamber lower slurry imports, 20. heating chamber lower slurry outlets, 21. mother liquor outlet, 22. vacuum evaporation crystallizer lower slurry imports, 23. mother liquor outlet, 24. vacuum evaporation crystallizer recycle pumps, 25. heating chamber lower slurry imports, 26. heating chamber lower slurry outlets, 27.DTB evaporative crystallizer lower slurry exports, 28. sodium sulfate slush pumps, 29. vacuum evaporation crystallizer lower slurry outlets, 30. sodium-chlor slush pumps, 31. No. two hydrocyclones, 32. sodium-chlor slurries buckets, 33. horizontal spiral centrifuges, 34. No. two mother liquor holding tanks, 35. No. two mother liquor pumps, 36. mother liquor outlet, 37. steam-ins, 38. steam-ins, 39. steam storage tanks, 40.MVR vapour compressor, 41. secondary steam outlets, 42. secondary steam outlets, 43. surface coolers, 44. water ring vacuum pumps, 45. steam separators, 46. cooling water tanks, 47. water coolant reuse tanks, 48. entrance of cooling water, 49. cooling water outlets, 50. condensation water tanks, 51. condensate pumps, 52. water of condensation storage tanks, 53. recycling condensing water pumps, 54.DTB evaporative crystallizer wire mesh demister rinse mouth, 55. vacuum evaporation crystallizer wire mesh demister rinse mouths, 56. mother liquor discharge outlets, 57. heating chamber vapor condensation water outs, 58. condensed water buckets, 59. heating chamber vapor condensation water outs, 60. condensed water buckets, 61. vapor condensation water pumps, 62. plate-type heat exchanger condensing water inlets, 63. plate-type heat exchanger condensation-water drains, 64.DTB evaporative crystallizer vertical-type axial-flow pump, 65. vacuum evaporation crystallizer vertical-type axial-flow pumps, 66.DTB evaporative crystallizer mother liquor room, 67. vacuum evaporation crystallizer mother liquor rooms.
Embodiment
Below in conjunction with accompanying drawing, the utility model is further described.
As shown in Figure 1, the utility model is high-concentration salt-containing wastewater MVR evaporative crystallization treatment system, comprise raw material storage tank 1, fresh feed pump 2, plate-type heat exchanger 3, DTB evaporative crystallizer heating chamber 4, DTB evaporative crystallizer 5, vacuum evaporation crystallizer heating chamber 6, vacuum evaporation crystallizer 7, a hydrocyclone 8, sodium sulfate slurries bucket 9, two-stage material-pushing centrifuge 10, vibrations fluid bed dryer 11, a mother liquor holding tank 12, a mother liquor pump 13, Recycling Mother Solution pump 14, it is characterized in that: described raw material storage tank 1 is linked in sequence fresh feed pump 2, plate-type heat exchanger 3, DTB evaporative crystallizer heating chamber 4, DTB evaporative crystallizer 5, vacuum evaporation crystallizer heating chamber 6, vacuum evaporation crystallizer 7, a hydrocyclone 8, sodium sulfate slurries bucket 9, two-stage material-pushing centrifuge 10, vibrations fluid bed dryer 11, a mother liquor holding tank 12, a mother liquor pump 13, Recycling Mother Solution pump 14, described plate-type heat exchanger 3 top is provided with plate-type heat exchanger serum outlet 15, plate-type heat exchanger serum outlet 15 is connected with DTB evaporative crystallizer lower slurry import 16 by pipeline, DTB evaporative crystallizer vertical-type axial-flow pump 64 is installed bottom DTB evaporative crystallizer 5, it is DTB evaporative crystallizer mother liquor room 66 in the middle part of DTB evaporative crystallizer 5, side, DTB evaporative crystallizer mother liquor room 66 is provided with mother liquor outlet 17, mother liquor outlet 17 is connected with DTB evaporative crystallizer recycle pump 18 by pipeline, DTB evaporative crystallizer recycle pump 18 is exported and is connected with heating chamber lower slurry import 19 by pipeline, heating chamber lower slurry outlet 20 is connected with DTB evaporative crystallizer lower slurry import 16 by pipeline, DTB evaporative crystallizer mother liquor room 66 opposite side is provided with mother liquor outlet 21, mother liquor outlet 21 is connected with vacuum evaporation crystallizer lower slurry import 22 by pipeline, DTB evaporative crystallizer lower slurry outlet 27 is connected with sodium sulfate slush pump 28 by pipeline, sodium sulfate slush pump 28 is connected with a hydrocyclone 8 by pipeline, a hydrocyclone 8 is arranged on sodium sulfate slurries bucket 9 top, sodium sulfate 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 a mother liquor holding tank 12, a mother liquor holding tank 12 is connected with a mother liquor pump 13 by pipeline, a mother liquor pump 13 is connected with Recycling Mother Solution pump 14 by pipeline, Recycling Mother Solution pump 14 is connected with DTB evaporative crystallizer lower slurry import 16 by pipeline one tunnel, another road is connected with mother liquor discharge outlet 56, vacuum evaporation crystallizer vertical-type axial-flow pump 65 is installed bottom vacuum evaporation crystallizer 7, it is vacuum evaporation crystallizer mother liquor room 67 in the middle part of vacuum evaporation crystallizer 7, side, vacuum evaporation crystallizer mother liquor room 67 is provided with mother liquor outlet 23, mother liquor outlet 23 is connected with vacuum evaporation crystallizer recycle pump 24 by pipeline, vacuum evaporation crystallizer recycle pump 24 is exported and is connected with heating chamber lower slurry import 25 by pipeline, heating chamber lower slurry outlet 26 is connected with vacuum evaporation crystallizer lower slurry import 22 by pipeline, vacuum evaporation crystallizer mother liquor room 67 opposite side is provided with mother liquor outlet 36, mother liquor outlet 36 is connected with Recycling Mother Solution pump 14 by pipeline, vacuum evaporation crystallizer lower slurry outlet 29 is connected with sodium-chlor slush pump 30 by pipeline, sodium-chlor slush pump 30 is connected with No. two hydrocyclones 31 by pipeline, No. two hydrocyclones 31 are arranged on sodium-chlor slurries bucket 32 top, sodium-chlor slurries bucket 32 is connected with horizontal spiral centrifuge 33 by pipeline, horizontal spiral centrifuge 33 is connected with No. two mother liquor holding tanks 34 by pipeline, No. two mother liquor holding tanks 34 are connected with No. two mother liquor pumps 35 by pipeline, No. two mother liquor pumps 35 are connected with vacuum evaporation crystallizer lower slurry import 22 by pipeline, DTB evaporative crystallizer heating chamber 4 top is provided with steam-in 37, steam-in 37 is connected with steam storage tank 39 by pipeline, vacuum evaporation crystallizer heating chamber 6 top is provided with steam-in 38, steam-in 38 is connected with steam storage tank 39 by pipeline, DTB evaporative crystallizer 5 top is provided with secondary steam outlet 41, secondary steam outlet 41 is connected with MVR vapour compressor 40 by pipeline, MVR vapour compressor 40 is provided with steam-in 37 by pipeline with DTB evaporative crystallizer heating chamber 4 top and is connected, vacuum evaporation crystallizer 7 top is provided with secondary steam outlet 42, secondary steam outlet 42 is connected with surface cooler 43 by pipeline, surface cooler 43 is connected with water ring vacuum pump 44 by pipeline, water ring vacuum pump 44 is connected with steam separator 45 by pipeline, side, surface cooler 43 bottom is provided with entrance of cooling water 48, opposite side is provided with cooling water outlet 49, entrance of cooling water 48 is connected with cooling water tank 46 by pipeline, cooling water outlet 49 is connected with water coolant reuse tank 47 by pipeline, be connected with condensation water tank 50 by pipeline bottom surface cooler 43, condensation water tank 50 is connected with condensate pump 51 by pipeline, condensate pump 51 is connected with water of condensation storage tank 52 by pipeline, water of condensation storage tank 52 is connected with recycling condensing water pump 53 by pipeline, recycling condensing water pump 53 is connected with DTB evaporative crystallizer wire mesh demister rinse mouth 54 by pipeline one tunnel, recycling condensing water pump 53 is connected with vacuum evaporation crystallizer wire mesh demister rinse mouth 55 by another road of pipeline, heating chamber vapor condensation water out 57 is provided with in the middle part of DTB evaporative crystallizer heating chamber 4, heating chamber vapor condensation water out 57 is connected with condensed water bucket 58 by pipeline, condensed water bucket 58 is connected with vapor condensation water pump 61 by pipeline, heating chamber vapor condensation water out 59 is provided with in the middle part of vacuum evaporation crystallizer heating chamber 6, heating chamber vapor condensation water out 59 is connected with condensed water bucket 60 by pipeline, condensed water bucket 60 is connected with vapor condensation water pump 61 by pipeline, vapor condensation water pump 61 is connected with plate-type heat exchanger condensing water inlet 62 by pipeline, plate-type heat exchanger condensation-water drain 63 is connected with water of condensation storage tank 52 by pipeline.
The know-why of native system be utilize sodium sulfate, the different solubility of sodium-chlor separated, during high temperature, the solubleness of sodium-chlor is large, and the solubleness of sodium sulfate is low, and sodium sulfate is separated out; During low temperature, the solubleness of sodium-chlor is little, and the solubleness of sodium sulfate is large, and sodium-chlor is separated out, and reaches the object that sodium-chlor is thoroughly separated with sodium sulfate, takes out respectively from different crystallizers, reaches the object of sodium sulfate, sodium-chlor separation.The solubility curve of sodium sulfate is retrograde solubility curve, and in 50 ~ 100 DEG C of intervals, along with the rising of temperature, solubleness reduces gradually, and the solubleness of sodium-chlor is positive solubility curve, in 50 ~ 110 DEG C of intervals.Along with the rising of temperature, solubleness strengthens gradually, and in native system, the crystallizer of sodium sulfate controls at 105 ~ 110 DEG C, and the crystallizer of sodium-chlor, at 50 ~ 55 DEG C, utilizes Recycling Mother Solution to be connected by the crystallizer of sodium sulfate and sodium-chlor respectively.During sulfate crystal, the solubleness of sodium-chlor increases non-crystallizable, can not separate out, ensure that the quality product of sodium sulfate, along with the circulation of mother liquor, arrived the crystallizer of sodium-chlor, the solubleness of sodium-chlor reduces, sodium-chlor crystallization, the solubleness of sodium sulfate increases, and does not separate out, ensure that the quality product of sodium-chlor.
Adopt DTB type evaporative crystallizer, vacuum evaporation crystallizer, because there is the mother liquor room compared with large regions in DTB type crystallizer, vacuum evaporation crystallizer, the nucleus of sodium-chlor or sodium sulfate can be separated with mother liquor in mother liquor room, the sodium-chlor contained in the mother liquor of supernatant liquor or metabisulfite solution are disposed to sodium-chlor or sulfate crystal system by the form that mother liquor discharges, effectively ensure that the quality of sodium sulfate, also ensure that the quality of sodium-chlor, to ensure in Recycling Mother Solution without nucleus thus to ensure the quality of product simultaneously.
Vertical-type axial-flow pump is the heart of crystallizer, and rotating speed is adjustable by frequency conversion, and alternatively uninterrupted can adjust, and degree of supersaturation size is adjustable, and nucleus quantity is adjustable, and therefore grain size number size also can adjust in certain scope.
MVR vapour compressor: adopt rare gas element and grease seal, completely independent with compressor impeller, can not leakage of oil, avoid the machine oil of compressor to bleed in material;
Adopt trash-type impeller; In order to ensure that the steam of compressor outlet is saturation steam (superheated vapour heat content is very low), a small amount of water need be sprayed to prevent steam superheating in the import of compressor.For unshrouded impeller, the water of spirt compressor can directly be beaten on impeller, because the rotating speed of impeller is very high, the globule is beaten on impeller, can cause very large impact to impeller, easily causes the transient equilibrium of compressor impeller unbalance, cause the cavitation erosion of compressor impeller, and the wearing and tearing of bearing.And for trash-type impeller, because impeller adopts two-sided shrouding, the water smoke that spirt goes can not directly be beaten on impeller, avoid the unbalance damage causing compressor of dynamic balance of impeller;
MVR vapour compressor technical parameter:
Air input 14.5 ~ 15.6t/h, inlet temperature: 100 DEG C, temperature out 116 DEG C, single-machine capacity 380KW, rotating speed 3586 revs/min, material: housing 316L, blade 2507.
Working process of the present utility model is: the alkali-wash waste water in the zinc recovering workshop (zinc oxide fumes wet processing output) in raw material storage tank 1 and electrodialysis output containing sodium sulfate, waste water (the flow 16.7t/h of sodium-chlor and other foreign ion, concentration of polymer solution 12.60%, wherein: sodium sulphate content accounts for 92%, sodium-chlor, Sodium Fluoride and other metal species account for 8%, original liquid temperature 25 DEG C), plate-type heat exchanger 3 is entered under fresh feed pump 2 acts on, carry out thermal pretreatment, sodium sulfate after preheating, the temperature of sodium chloride waste water is 50 DEG C, pressure 0.28MPa, then DTB evaporative crystallizer heating chamber 4 is entered, from the 0.7MPa of steam storage tank 39, the saturation steam of 170 DEG C, enter DTB evaporative crystallizer heating chamber 4, to sodium sulfate, sodium chloride waste water heats, before DTB evaporative crystallizer starts, disposablely pass into saturation steam, after treating feed liquid boiling, secondary steam employing MVR vapour compressor 40 carries out compression cycle utilization, does not re-use saturation steam,
After heating, sodium sulfate, sodium chloride waste water became hot solution, then enter DTB evaporative crystallizer 5 evaporative crystallization, the temperature of control DTB evaporative crystallizer is at 105 ~ 110 DEG C, and during sulfate crystal, the solubleness of sodium-chlor increases non-crystallizable, can not separate out, ensure that the quality product of sodium sulfate;
Along with the circulation of mother liquor, arrived vacuum evaporation crystallizer 7, controlled the temperature of vacuum evaporation crystallizer 7 at 50 ~ 55 DEG C, the solubleness of sodium-chlor reduces, sodium-chlor crystallization, and the solubleness of sodium sulfate increases, and does not separate out, ensure that the quality product of sodium-chlor;
Sodium sulfate crystal natural subsidence in DTB evaporative crystallizer 5 is below crystallizer, a hydrocyclone 8 is sent into by sodium sulfate slush pump 28, under the effect of a hydrocyclone 8, slurries export from a hydrocyclone 8 and flow out, enter sodium sulfate slurries bucket 9, then enter two-stage material-pushing centrifuge 10 and carry out solid-liquid separation, Na
2sO
4xln flows out from two-stage material-pushing centrifuge 10, enter vibrations fluid bed dryer 11 and carry out drying treatment, anhydrous sodium sulphate (1690Kg/h) quality finally obtained reaches the requirement of GB/T6009-2014 " industrial anhydrous sodium sulfate " II class acceptable end product, wherein sodium sulphate content>=98%; Slurries flow into a mother liquor holding tank 12 from two-stage material-pushing centrifuge 10 serum outlet, and mother liquor enters DTB evaporative crystallization by a mother liquor pump 13 from DTB evaporative crystallizer lower slurry import 16; The a small amount of mother liquor of another part regularly controls the enrichment in evaporative crystallizer of fluorion, calcium ions and magnesium ions to the discharge of prime pretreatment system;
Sodium chloride crystal natural subsidence in vacuum evaporation crystallizer 7 is below crystallizer, No. two hydrocyclones 31 are sent into by sodium-chlor slush pump 30, under the effect of No. two hydrocyclones 31, slurries export from No. two hydrocyclones 31 and flow out, enter sodium-chlor slurries bucket 32, then enter horizontal spiral centrifuge 33 and carry out solid-liquid separation, NaCl xln flows out from horizontal spiral centrifuge 33, industrial chlorinations sodium (147Kg/h) quality of evaporative crystallization reaches the refining sodium-chlor secondary standard requirement of (GBT5462-2003) National Industrial sodium-chlor standard-required, i.e. NaCl >=97.5%, granularity >=0.8mm, uniform particles, any surface finish, slurries flow into No. two mother liquor holding tanks 34 from horizontal spiral centrifuge 33 serum outlet, and mother liquor enters vacuum evaporation crystallizer by No. two mother liquor pumps 35 from vacuum evaporation crystallizer lower slurry import 22,
Simultaneously from vacuum evaporation crystallizer 7 water vapor (temperature is 46 DEG C, pressure-0.09MPa) out, enter surface cooler 43, after cooling, (temperature is 42 DEG C, pressure 0.2MPa), enter condensation water tank 50, send into water of condensation storage tank 52 through condensate pump 51;
Enter surface cooler 43 from the water coolant (temperature is 32 DEG C, pressure 0.38MPa) of cooling water tank 46, after heat exchange (temperature is 42 DEG C, pressure 0.2MPa), then enter water coolant reuse tank 47;
Enter condensed water bucket 58 from DTB evaporative crystallizer heating chamber 4 steam condensate (temperature is 90 DEG C, pressure 0.15MPa) out, enter plate-type heat exchanger 3 by vapor condensation water pump 61; Enter condensed water bucket 60 from vacuum evaporation crystallizer heating chamber 6 steam condensate (temperature is 54 DEG C, pressure 0.075MPa) out, enter plate-type heat exchanger 3 by vapor condensation water pump 61;
After heat exchange, (temperature is 48 DEG C, pressure 0.08MPa) enter water of condensation storage tank 52, DTB evaporative crystallizer wire mesh demister rinse mouth 54, vacuum evaporation crystallizer wire mesh demister rinse mouth 55 is sent into through recycling condensing water pump 53, rinse DTB evaporative crystallizer 5, vacuum evaporation crystallizer 7, water of condensation obtains reuse;
As can be seen here, the utility model high-concentration salt-containing wastewater MVR evaporative crystallization treatment system, this system is disposable before DTB evaporative crystallizer starts passes into saturation steam, after treating feed liquid boiling, secondary steam adopts vapour compression pump to carry out compression cycle utilization, do not re-use saturation steam, energy efficient, reach energy-conservation object, will containing sodium sulfate by MVR evaporation and crystallization system, the waste water evaporative crystallization of sodium-chlor and other foreign ion, sodium sulfate and sodium-chlor are separated, the anhydrous sodium sulphate quality finally obtained reaches the requirement of GB/T6009-2014 " industrial anhydrous sodium sulfate " II class acceptable end product, wherein sodium sulphate content >=98%, industrial chlorinations sodium reaches Exposure to Sunlight sodium-chlor secondary standard requirement in National Industrial sodium-chlor standard (GBT5462-2003), all the other heavy metals and other metal ions by mother liquor regularly or continuous print form of export be disposed to prime pretreatment system.System synthesis energy consumption is low; Not plugging, non-scaling, grain size number is large, smooth appearance.
Claims (1)
1. high-concentration salt-containing wastewater MVR evaporative crystallization treatment system, comprise raw material storage tank, fresh feed pump, plate-type heat exchanger, DTB evaporative crystallizer heating chamber, DTB evaporative crystallizer, vacuum evaporation crystallizer heating chamber, vacuum evaporation crystallizer, a hydrocyclone, sodium sulfate slurries bucket, two-stage material-pushing centrifuge, vibrations fluid bed dryer, a mother liquor holding tank, a mother liquor pump, Recycling Mother Solution pump, it is characterized in that: described raw material storage tank is linked in sequence fresh feed pump, plate-type heat exchanger, DTB evaporative crystallizer heating chamber, DTB evaporative crystallizer, vacuum evaporation crystallizer heating chamber, vacuum evaporation crystallizer, a hydrocyclone, sodium sulfate slurries bucket, two-stage material-pushing centrifuge, vibrations fluid bed dryer, a mother liquor holding tank, a mother liquor pump, Recycling Mother Solution pump, described plate-type heat exchanger top is provided with plate-type heat exchanger serum outlet, plate-type heat exchanger serum outlet is connected with the import of DTB evaporative crystallizer lower slurry by pipeline, DTB evaporative crystallizer vertical-type axial-flow pump is installed bottom DTB evaporative crystallizer, it is DTB evaporative crystallizer mother liquor room in the middle part of DTB evaporative crystallizer, side, DTB evaporative crystallizer mother liquor room is provided with mother liquor outlet, mother liquor outlet is connected with DTB evaporative crystallizer recycle pump by pipeline, DTB evaporative crystallizer circulating-pump outlet is connected with the import of heating chamber lower slurry by pipeline, the outlet of heating chamber lower slurry is connected with the import of DTB evaporative crystallizer lower slurry by pipeline, DTB evaporative crystallizer mother liquor room opposite side is provided with mother liquor outlet, mother liquor outlet is connected with the import of vacuum evaporation crystallizer lower slurry by pipeline, the outlet of DTB evaporative crystallizer lower slurry is connected with sodium sulfate slush pump by pipeline, sodium sulfate slush pump is connected with a hydrocyclone by pipeline, a hydrocyclone is arranged on sodium sulfate slurries bucket top, sodium sulfate 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 a mother liquor holding tank, a mother liquor holding tank is connected with a mother liquor pump by pipeline, a mother liquor pump is connected with Recycling Mother Solution pump by pipeline, Recycling Mother Solution pump is connected with the import of DTB evaporative crystallizer lower slurry by pipeline one tunnel, another road is connected with mother liquor discharge outlet, vacuum evaporation crystallizer vertical-type axial-flow pump is installed bottom vacuum evaporation crystallizer, it is vacuum evaporation crystallizer mother liquor room in the middle part of vacuum evaporation crystallizer, side, vacuum evaporation crystallizer mother liquor room is provided with mother liquor outlet, mother liquor outlet is connected with vacuum evaporation crystallizer recycle pump by pipeline, vacuum evaporation crystallizer circulating-pump outlet is connected with the import of heating chamber lower slurry by pipeline, the outlet of heating chamber lower slurry is connected with the import of vacuum evaporation crystallizer lower slurry by pipeline, vacuum evaporation crystallizer mother liquor room opposite side is provided with mother liquor outlet, mother liquor outlet is connected with Recycling Mother Solution pump by pipeline, the outlet of vacuum evaporation crystallizer lower slurry is connected with sodium-chlor slush pump by pipeline, sodium-chlor slush pump is connected with No. two hydrocyclones by pipeline, No. two hydrocyclones are arranged on sodium-chlor slurries bucket top, sodium-chlor slurries bucket is connected with horizontal spiral centrifuge by pipeline, horizontal spiral centrifuge is connected with No. two mother liquor holding tanks by pipeline, No. two mother liquor holding tanks are connected with No. two mother liquor pumps by pipeline, No. two mother liquor pumps are connected with the import of vacuum evaporation crystallizer lower slurry by pipeline, DTB evaporative crystallizer heating chamber top is provided with steam-in, steam-in is connected with steam storage tank by pipeline, vacuum evaporation crystallizer heating chamber top is provided with steam-in, steam-in is connected with steam storage tank by pipeline, DTB evaporative crystallizer top is provided with secondary steam outlet, secondary steam outlet is connected with MVR vapour compressor by pipeline, MVR vapour compressor is provided with steam-in by pipeline with DTB evaporative crystallizer heating chamber top and is connected, vacuum evaporation crystallizer top is provided with secondary steam outlet, secondary steam outlet is connected with surface cooler by pipeline, surface cooler is connected with water ring vacuum pump by pipeline, water ring vacuum pump is connected with steam separator by pipeline, side, surface cooler bottom is provided with entrance of cooling water, opposite side is provided with cooling water outlet, entrance of cooling water is connected with cooling water tank by pipeline, cooling water outlet is connected with water coolant reuse tank by pipeline, be connected with condensation water tank by pipeline bottom surface cooler, condensation water tank is connected with condensate pump by pipeline, condensate pump is connected with water of condensation storage tank by pipeline, water of condensation storage tank is connected with recycling condensing water pump by pipeline, recycling condensing water pump is connected with DTB evaporative crystallizer wire mesh demister rinse mouth by pipeline one tunnel, recycling condensing water pump is connected with vacuum evaporation crystallizer wire mesh demister rinse mouth by another road of pipeline, heating chamber vapor condensation water out is provided with in the middle part of DTB evaporative crystallizer heating chamber, 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, heating chamber vapor condensation water out is provided with in the middle part of vacuum evaporation crystallizer heating chamber, 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520873716.2U CN205099538U (en) | 2015-11-02 | 2015-11-02 | High concentration contains salt waste water MVR evaporation crystallization process system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520873716.2U CN205099538U (en) | 2015-11-02 | 2015-11-02 | High concentration contains salt waste water MVR evaporation crystallization process system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205099538U true CN205099538U (en) | 2016-03-23 |
Family
ID=55515329
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520873716.2U Expired - Fee Related CN205099538U (en) | 2015-11-02 | 2015-11-02 | High concentration contains salt waste water MVR evaporation crystallization process system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205099538U (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105859003A (en) * | 2016-05-06 | 2016-08-17 | 武汉宏澳绿色能源工程有限责任公司 | Method and device for salt separation and crystallization of high-salinity wastewater in coal chemical industry |
| CN106288869A (en) * | 2016-09-21 | 2017-01-04 | 天津科技大学 | The elimination superheater of mechanical compression type heat pump outlet vapor |
| CN108079607A (en) * | 2017-12-25 | 2018-05-29 | 合肥恒力装备有限公司 | A kind of evaporative crystallization anti-block apparatus |
| WO2018126651A1 (en) * | 2017-01-05 | 2018-07-12 | 广州市心德实业有限公司 | Evaporation, crystallization and drying integrated device and evaporation crystallization drying method |
| CN109607923A (en) * | 2019-01-07 | 2019-04-12 | 揭阳市德克蒸发器有限公司 | A kind of heat pump low temperature divides the wastewater treatment equipment of salt |
| CN112401926A (en) * | 2020-10-23 | 2021-02-26 | 宋娟 | Combined examination and diagnosis device for ultrasound department |
-
2015
- 2015-11-02 CN CN201520873716.2U patent/CN205099538U/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105859003A (en) * | 2016-05-06 | 2016-08-17 | 武汉宏澳绿色能源工程有限责任公司 | Method and device for salt separation and crystallization of high-salinity wastewater in coal chemical industry |
| CN106288869A (en) * | 2016-09-21 | 2017-01-04 | 天津科技大学 | The elimination superheater of mechanical compression type heat pump outlet vapor |
| WO2018126651A1 (en) * | 2017-01-05 | 2018-07-12 | 广州市心德实业有限公司 | Evaporation, crystallization and drying integrated device and evaporation crystallization drying method |
| CN108079607A (en) * | 2017-12-25 | 2018-05-29 | 合肥恒力装备有限公司 | A kind of evaporative crystallization anti-block apparatus |
| CN109607923A (en) * | 2019-01-07 | 2019-04-12 | 揭阳市德克蒸发器有限公司 | A kind of heat pump low temperature divides the wastewater treatment equipment of salt |
| CN112401926A (en) * | 2020-10-23 | 2021-02-26 | 宋娟 | Combined examination and diagnosis device for ultrasound department |
| CN112401926B (en) * | 2020-10-23 | 2024-04-12 | 宋娟 | Combined type examination and diagnosis device for ultrasonic department |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN205099538U (en) | High concentration contains salt waste water MVR evaporation crystallization process system | |
| CN104803535B (en) | A kind of recovery system and recovery process for reclaiming salt from desulfurization wastewater | |
| CN103203116B (en) | A kind of MVR continuous evaporative crystallization system and continuous evaporative crystallization method | |
| CN103007553B (en) | A kind of function of mechanical steam recompression continuous evaporative crystallization system and method | |
| CN204034294U (en) | The board-like forced-circulation evaporator of novel triple effect | |
| CN207748878U (en) | A kind of recovery and processing system for sodium sulphate in high-salt wastewater | |
| CN205099370U (en) | High concentration contains salt waste water evaporation crystallization process device | |
| CN205773844U (en) | A kind of high-salt wastewater triple effect evaporation crystallization apparatus without cooling down water | |
| CN203836931U (en) | Centralized-packing closed type high temperature steam condensate water recovery system | |
| CN103394206B (en) | High-efficiency energy-saving hydrochloric acid pickling waste liquor triple-effect negative-pressure graphite evaporation crystallizer | |
| CN110422899A (en) | A kind of heat pump flash vaporization concentration systems | |
| CN111362492A (en) | Double-effect MVR evaporation treatment method | |
| CN209286688U (en) | MVR evaporator replaces the Production of Barium Chloride system of traditional four-effect evaporator | |
| CN203436836U (en) | Efficient and energy-saving type three-effect negative-pressure graphite evaporative crystallization device of hydrochloric acid pickling waste liquid | |
| CN203591603U (en) | Sextuple-effect evaporator | |
| CN204588909U (en) | A kind of recovery system reclaiming salt from desulfurization wastewater | |
| CN110171900A (en) | A kind of high temperature brine waste concentration and crystallization device and application | |
| CN203820492U (en) | Continuous wastewater evaporation-concentration-crystallization device | |
| CN205099397U (en) | High concentration sulfur acid sodium waste water evaporation crystallization process device | |
| CN203095629U (en) | Sodium chloride recycling and crystallizing device | |
| CN205099371U (en) | High concentration contains sodium chloride waste water evaporation crystallization process device | |
| CN211971803U (en) | Novel materialized wastewater triple-effect evaporation system | |
| CN106587479A (en) | Industrial electroplating wastewater zero-discharge treatment equipment and treatment process thereof | |
| CN107840399A (en) | Rotary evaporator and low-temperature evaporation condensing crystallizing equipment | |
| CN207845410U (en) | A kind of zinc borate production wastewater treatment equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160323 Termination date: 20171102 |