CN221028018U - Sodium sulfate wastewater separation and refining system containing organic matters easy to change color - Google Patents
Sodium sulfate wastewater separation and refining system containing organic matters easy to change color Download PDFInfo
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- CN221028018U CN221028018U CN202322853886.1U CN202322853886U CN221028018U CN 221028018 U CN221028018 U CN 221028018U CN 202322853886 U CN202322853886 U CN 202322853886U CN 221028018 U CN221028018 U CN 221028018U
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- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 title claims abstract description 37
- 229910052938 sodium sulfate Inorganic materials 0.000 title claims abstract description 37
- 235000011152 sodium sulphate Nutrition 0.000 title claims abstract description 37
- 239000002351 wastewater Substances 0.000 title claims abstract description 23
- 230000008859 change Effects 0.000 title claims abstract description 22
- 238000000926 separation method Methods 0.000 title claims abstract description 21
- 238000007670 refining Methods 0.000 title claims abstract description 11
- 239000013078 crystal Substances 0.000 claims abstract description 32
- 239000002002 slurry Substances 0.000 claims abstract description 32
- 239000000243 solution Substances 0.000 claims abstract description 24
- 238000002156 mixing Methods 0.000 claims abstract description 17
- 239000002562 thickening agent Substances 0.000 claims abstract description 15
- 239000011229 interlayer Substances 0.000 claims abstract description 14
- 238000001035 drying Methods 0.000 claims abstract description 11
- 238000005406 washing Methods 0.000 claims abstract description 11
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 10
- 239000007791 liquid phase Substances 0.000 claims abstract description 9
- 239000007790 solid phase Substances 0.000 claims abstract description 5
- 239000010413 mother solution Substances 0.000 claims abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 28
- 239000012452 mother liquor Substances 0.000 claims description 12
- 238000007599 discharging Methods 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 4
- 238000002347 injection Methods 0.000 claims description 3
- 239000007924 injection Substances 0.000 claims description 3
- 239000007788 liquid Substances 0.000 abstract description 33
- 150000003839 salts Chemical class 0.000 abstract description 24
- 238000011084 recovery Methods 0.000 abstract description 4
- 238000010924 continuous production Methods 0.000 abstract description 2
- 238000002845 discoloration Methods 0.000 abstract description 2
- 239000000463 material Substances 0.000 description 12
- 238000001704 evaporation Methods 0.000 description 10
- 230000008020 evaporation Effects 0.000 description 10
- 239000000428 dust Substances 0.000 description 8
- 238000000034 method Methods 0.000 description 8
- 239000000047 product Substances 0.000 description 8
- 239000011552 falling film Substances 0.000 description 7
- 239000005416 organic matter Substances 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- 239000002699 waste material Substances 0.000 description 7
- 239000002910 solid waste Substances 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical class O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 238000002425 crystallisation Methods 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000001953 recrystallisation Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 230000008719 thickening Effects 0.000 description 2
- 208000034874 Product colour issue Diseases 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 210000003437 trachea Anatomy 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
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- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The utility model discloses a sodium sulfate wastewater separation and refining system containing organic matters easy to change color, wherein a cone bucket is sleeved at the lower part of a barrel body of a crystallizer to form an annular interlayer and is provided with a concentrated solution outlet, and the lower end of the cone bucket is connected with a washing barrel; the reducing agent and the pH regulator enter a feeding and blending tank, a feeding and blending liquid is connected with a elutriation port of a crystallizer through a condensate preheater, an elutriation crystal slurry outlet is connected with a thickener and a crystal slurry centrifuge, and a crystal slurry solid phase outlet is connected with a drying bed through a screw conveyor; the concentrated solution outlet is connected to a degumming kettle and a degumming centrifuge, the degumming liquid phase outlet, the crystal slurry centrifuge liquid phase outlet and the thickener overflow are respectively connected with a mother solution tank, the outlet of the mother solution tank is connected with a circulating pipe of a crystallizer, the circulating pipe of the crystallizer is connected with a pipe side inlet of a heater through a circulating pump, and the pipe side outlet of the heater is connected with a circulating inlet of the crystallizer. The system can reduce the discoloration of crystallized salt, improve the quality of the product salt, increase the recovery rate of the product salt and improve the continuous production capacity of the device.
Description
Technical Field
The utility model relates to a sodium sulfate wastewater separation and refining system, in particular to a sodium sulfate wastewater separation and refining system containing organic matters easy to change color, belonging to the technical field of waste salt separation and refining.
Background
The existing sodium sulfate waste salt containing the organic matters easy to change color generally adopts a technology of impurity removal and multiple-effect crystallization, solid waste is generated, organic matters in waste water in the impurity removal process are not thoroughly removed, the obtained sodium sulfate waste water containing the organic matters easy to change color is concentrated by evaporation, the concentration of the organic matters easy to change color is increased, the sodium sulfate product obtained by crystallization can not be reused as industrial salt due to the fact that the mixed organic matters are easy to oxidize and change color when contacting with air, the purity is lower, the sodium sulfate product can only be generally used as dangerous solid waste to be disposed, and the national disposal requirement on the dangerous solid waste is extremely strict, so that the production cost of enterprises is greatly improved.
The enrichment of organic matters in the conventional evaporation process has a large influence on the temperature rise of the evaporation boiling point, and the device is difficult to continuously produce. The evaporation is usually maintained by removing saturated brine containing high-concentration organic matters, so that the pressure of a subsequent environment-friendly treatment unit is greatly increased, the impact and even the system breakdown of the environment-friendly biochemical treatment are caused by excessive salt, and the discharged saturated brine is wasted by a large amount of inorganic salt, so that the saturated brine becomes a constraint factor affecting the normal production of enterprises.
The Chinese patent publication No. CN 106395949B discloses a sodium sulfate wastewater treatment system, which comprises an effective falling film evaporator, wherein an outlet of a sodium sulfate wastewater pipe is connected with a feed liquid inlet at the lower part of the effective falling film evaporator through a feed pump, a steam inlet at the upper part of a shell side of the effective falling film evaporator is connected with a steam supply pipe, and a condensed water outlet at the lower part of the shell side of the effective falling film evaporator is connected with an effective condensed water pipe; the material separating port at the lower part of the first-effect falling film evaporator is connected with the first-effect separator through a communicating pipe, the first-effect separator steam exhaust port at the top of the first-effect separator is connected with the first-effect separator steam exhaust pipe, the material liquid outlet at the bottom of the first-effect separator and the material liquid outlet at the bottom of the first-effect falling film evaporator are connected with the inlet of a first-effect circulating pump together, the outlet of the first-effect circulating pump is connected with the circulating liquid inlet at the top of the first-effect falling film evaporator through a first-effect circulating pipe, and the outlet of the first-effect circulating pump is also connected with a first-effect material liquid output pipe. The system can not solve the problem of removing the organic matters easy to change color, and the energy consumption is still higher.
In summary, the conventional evaporative crystallization existing at present has the advantages of large pollution discharge amount, low recovery rate, easy product discoloration, low quality and short continuous operation time of the device. How to realize the refining production of sodium sulfate brine containing easy-to-change organic matters becomes a problem which needs to be solved urgently, and also restricts the development of the environmental protection industry.
Disclosure of utility model
The utility model aims to overcome the problems in the prior art and provide a sodium sulfate wastewater separation and refining system containing organic matters easy to change color, which can reduce the color change of crystal salt, improve the quality of product salt, increase the salt recovery rate of the product and improve the continuous production capacity of a device.
In order to solve the technical problems, the sodium sulfate wastewater separation and refining system comprises a feeding blending tank and a crystallizer, wherein the lower part of a cylinder body of the crystallizer is provided with a cone hopper, the upper port of the cone hopper is sleeved on the periphery of the cylinder body to form an annular interlayer, the side wall of the annular interlayer is provided with a concentrated solution outlet, and the lower end of the cone hopper is connected with a washing cylinder;
The outlet of the reducing agent and the pH regulator is connected to a feeding blending tank, the outlet of the feeding blending tank is connected with the cold side inlet of a condensate preheater through a feeding pump, the cold side outlet of the condensate preheater is connected with a elutriation port on the side wall of the elutriation cylinder, the crystal slurry outlet on the lower part of the elutriation cylinder is connected with the inlet of a thickener through a discharging pump, the underflow outlet of the thickener is connected with the inlet of a crystal slurry centrifuge, and the solid phase outlet of the crystal slurry centrifuge is connected with a drying bed through a screw conveyor;
The concentrated solution outlet of the crystallizer is connected with the inlet of the degumming kettle through a concentrated solution pump, the bottom outlet of the degumming kettle is connected with the inlet of a degumming centrifuge, and the liquid phase outlet of the degumming centrifuge is connected with a mother solution tank;
The liquid phase outlet of the crystal slurry centrifugal machine is connected with the overflow port of the thickener respectively with the inlet of the mother liquor tank, the outlet of the mother liquor tank is connected with the circulating pipe of the crystallizer through the mother liquor pump, the circulating pipe of the crystallizer is connected with the pipe side inlet of the heater through the circulating pump, and the pipe side outlet of the heater is connected with the circulating inlet of the crystallizer.
As an improvement of the utility model, a secondary steam outlet at the top of the crystallizer is connected with an inlet of a primary steam compressor through a secondary separator, an outlet of the primary steam compressor is connected with an inlet of a secondary steam compressor, an outlet of the secondary steam compressor is connected with a shell side inlet of the heater, a shell side outlet of the heater is connected with an inlet of a condensate water tank, and an outlet of the condensate water tank is connected with a hot side inlet of the condensate water preheater through a condensate water pump.
As a further improvement of the utility model, the outlets of the primary vapor compressor and the secondary vapor compressor are respectively provided with a condensed water injection port.
Compared with the prior art, the utility model has the following beneficial effects: 1. the system adopts the technologies of medicament shielding, on-line degumming, crystallizer structure optimization and the like, is suitable for sodium sulfate wastewater treatment containing the organic matters easy to change color, realizes the recycling of waste salt, achieves the purposes of energy conservation and emission reduction, changes waste into valuables, improves the production economy, provides a safe, energy-saving and environment-friendly treatment means for the sodium sulfate wastewater treatment containing the organic matters easy to change color, and provides a new method and a new idea for the recycling of the waste salt;
2. The system rapidly mixes and reacts the wastewater containing the organic matters easy to change color with the reducing agent and the pH regulator, reduces the pH value of the wastewater, improves the reducibility, shields the oxidation of the organic matters easy to change color in the transportation of the wastewater, slows down the oxidation degree in the evaporation process, and improves the continuity of the system operation;
3. In the system, the material inlet of the crystallizer is arranged at the lateral direction, and the circulating material liquid enters the straight section of the crystallizer along the lateral direction, so that the material updating speed at the liquid level is increased, the rate of converting water vapor from liquid phase to vapor phase is improved, the vapor-liquid separation efficiency is improved, the size of equipment is reduced, and the investment is reduced;
4. The lower cone of the crystallizer is provided with a washing cylinder, the washing cylinder is provided with a washing opening, waste water enters the system from the washing opening and forms a reverse flow field with sodium sulfate crystal slurry in the washing cylinder, the opportunity content of the new waste water is relatively low, the organic matter content in the sodium sulfate crystal slurry after washing is reduced, the entrainment of organic matters in the crystal slurry is reduced, the quality of salt is improved, sodium sulfate produced after drying meets the requirements of class II first products of industrial salt GBT6009-2014, the solid waste treated at the expense is converted into recyclable products, and the environment-friendly value and economic benefit are extremely high;
5. The lower part of the straight section of the crystallizer is provided with an annular interlayer, the center of the crystallizer is downward flowing crystal slurry, the inner side of the interlayer is upward flowing high-concentration organic concentrated solution, so that the high-concentration organic concentrated solution has small flow rate, small rising flow rate and no crystal particles, the organic content of the concentrated solution is high, the top of the interlayer is provided with a high-concentration organic concentrated solution outlet, the maximum discharge of the high-concentration organic matters can be realized, the organic matter enrichment speed of an evaporation system and the organic matter content in the system are greatly reduced, the quality of crystallized salt is improved, the continuous operation time of the system is prolonged, and meanwhile, a vapor/liquid separation system is converted into a vapor/liquid/concentrated solution separation system, so that a new idea is provided for three separation of materials;
6. The high-concentration organic concentrated solution of the crystallizer is subjected to online removal by an external degumming kettle, and then clear liquid flows back, so that the continuous operation of the evaporation system can be ensured, the waste caused by insufficient energy consumption and equipment utilization rate due to frequent start-up and shutdown is avoided, a large amount of liquid waste is converted into a small amount of solid waste by external degumming, the reduction of organic waste is realized, the treatment cost and difficulty are reduced, the economic benefit is extremely high, and a new means is provided for the stable operation of the evaporation system and online impurity removal;
7. Compared with the single-stage compressor of the traditional process, the rotating speed is 12000-16000 r/min under the same working condition, so that the noise is large, the safety coefficient is low, the adjustable operation interval is narrow, and the continuous operation stability is poor; the steam compressors used in the system are connected in series in two stages, the steam outlet of the primary compressor is connected with the steam inlet of the secondary compressor, and the steam outlet of the secondary compressor is connected with the inlet of the evaporator, so that compared with the traditional single-machine compressor, the two-stage compressor can realize higher pressure ratio and lower rotating speed, and can realize wider adjusting range by variable frequency adjustment, thereby greatly reducing environmental noise, improving the operating environment and reducing the operating energy consumption and equipment loss while meeting the operating conditions;
8. Through elutriation of crystal mush and thickening of a thickener, the granularity of sodium sulfate is further improved, the solid-liquid ratio entering a centrifugal machine is improved to 35-45%, compared with the traditional process, the salt liquid content of centrifugal separation is reduced to below 2%, the energy consumption of a dry bed is effectively reduced, and the quality of a final product is further improved;
9. And sodium sulfate wet salt produced by the crystal slurry centrifugal machine is conveyed by using a screw conveyor, salt scattering in the conveying process is reduced, the screw conveyor is provided with a reversing mode, and the reversing mode is used for reversing when the centrifugal machine is cleaned, so that the influence of centrifugal flushing water on a fluidized bed is effectively prevented, and the running stability of a drying bed is improved.
Drawings
The utility model will now be described in further detail with reference to the drawings and the detailed description, which are provided for reference and illustration only and are not intended to limit the utility model.
FIG. 1 is a flow chart of a sodium sulfate wastewater separation and purification system containing an organic matter with easy color change;
FIG. 2 is a schematic diagram of a crystallizer according to the present utility model;
In the figure: 1. a feed blending tank; 2. a reducing agent dosing tank; 3. a condensate preheater; 4. a crystallizer; 5. a heater; 6. a secondary separator; 7. a first stage vapor compressor; 8. a second-stage vapor compressor; 9. a condensate water tank; 10. a surface cooler; 11. a vacuum pump unit; 12. a degumming kettle; 13. degumming a centrifuge; 14. a thickener; 15. a magma centrifuge; 16. a mother liquor tank; 17. a screw conveyor; 18. a drying bed; 19. a blower; 20. a fin heat exchanger; 21. a cyclone dust collector; 22. a bag-type dust collector; 23. an induced draft fan;
And (3) a crystallizer: k1. a circulation inlet; k2. a circulation outlet; k3. washing the mouth; k4. a slurry sidewall outlet; k5. a crystal slurry bottom outlet; k6. a concentrate outlet; K7. a secondary steam outlet;
B1. A feed pump; B2. a circulation pump; B3. a concentrate pump; B4. a discharge pump; B5. a mother liquid pump; B6. a condensate pump; G1. a feed pipe; G2. a steam generating pipe; G3. a condenser water pipe; G4. the trachea is not condensed.
Detailed Description
In the following description of the present utility model, the terms "upper", "lower", "front", "rear", "left", "right", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are merely for convenience in describing the present utility model and simplifying the description, and do not mean that the device must have a specific orientation.
The utility model is further described with reference to the following detailed drawings in order to make the technical means, the creation characteristics, the achievement of the purpose and the effect of the implementation of the utility model easy to understand.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this utility model belongs. The terminology used herein in the description of the utility model is for the purpose of describing particular embodiments only and is not intended to be limiting of the utility model.
As shown in figure 1, the sodium sulfate wastewater separation and refining system containing the organic matters easy to change color comprises a feeding and blending tank 1, a reducing agent blending tank 2, a condensate preheater 3, a crystallizer 4, a heater 5, a secondary separator 6, a primary steam compressor 7, a secondary steam compressor 8, a degumming kettle 12, a degumming centrifugal machine 13, a thickener 14, a crystal slurry centrifugal machine 15, a mother liquor tank 16, a screw conveyer 17 and a drying bed 18, wherein a cone hopper is arranged at the lower part of a barrel of the crystallizer 4, an upper port of the cone hopper is sleeved on the periphery of the barrel to form an annular interlayer, a concentrated solution outlet is arranged on the side wall of the annular interlayer, and the lower end of the cone hopper is connected with a washing barrel;
The outlet of the reducing agent and the pH regulator is connected into a feeding blending tank 1, the outlet of the feeding blending tank 1 is connected with the cold side inlet of a condensate preheater 3 through a feeding pump, the cold side outlet of the condensate preheater 3 is connected with a elutriation port on the side wall of an elutriation cylinder, the crystal slurry outlet on the lower part of the elutriation cylinder is connected with the inlet of a thickener 14 through a discharging pump, the underflow outlet of the thickener 14 is connected with the inlet of a crystal slurry centrifuge 15, and the solid phase outlet of the crystal slurry centrifuge 15 is connected with a drying bed 18 through a screw conveyor 17;
The concentrated solution outlet of the crystallizer 4 is connected with the inlet of the degumming kettle 12 through a concentrated solution pump, the bottom outlet of the degumming kettle 12 is connected with the inlet of a degumming centrifuge 13, and the liquid phase outlet of the degumming centrifuge 13 is connected with a mother liquor tank 16;
The liquid phase outlet of the crystal slurry centrifuge 15 and the overflow port of the thickener 14 are respectively connected with the inlet of the mother liquor tank 16, the outlet of the mother liquor tank 16 is connected with the circulating pipe of the crystallizer 4 through a mother liquor pump, the circulating pipe of the crystallizer 4 is connected with the pipe side inlet of the heater 5 through a circulating pump, and the pipe side outlet of the heater 5 is connected with the circulating inlet of the crystallizer 4.
The secondary steam outlet at the top of the crystallizer 4 is connected with the inlet of a primary steam compressor 7 through a secondary separator 6, the outlet of the primary steam compressor 7 is connected with the inlet of a secondary steam compressor 8, the outlet of the secondary steam compressor 8 is connected with the shell side inlet of a heater 5, the shell side outlet of the heater 5 is connected with the inlet of a condensate water tank 9, and the outlet of the condensate water tank 9 is connected with the hot side inlet of the condensate water preheater 3 through a condensate water pump.
The outlets of the primary steam compressor 7 and the secondary steam compressor 8 are respectively provided with a condensed water injection inlet, and the shell side inlet of the heater 5 is also connected with a raw steam pipe.
Sodium sulfate wastewater containing the organic matters easy to change color from a feed pipe G1 enters a feed blending tank 1, the reducing agent in a reducing agent blending tank 2 is also put into the feed blending tank 1, the adding proportion of the reducing agent is 0.05 percent by weight, and a pH regulator is also added into the feed blending tank 1 to blend the pH value to 5.5-6.0, so that the oxidation color change degree in the conveying and subsequent evaporation processes is slowed down. The feed pump B1 sends the prepared feed liquid to the cold side of the condensate preheater 3, after the feed liquid is preheated to 75 ℃, the feed liquid enters the crystallizer 4 from the elutriation port k3, and simultaneously, the fine sodium sulfate and the concentrated liquid in the elutriation cylinder at the bottom of the crystallizer 4 are brought back to the evaporation system.
The feed liquid in the crystallizer 4 flows out from a circulating outlet K2, is sent into a heater 5 through a circulating pump B2 to be heated to 88-92 ℃, then enters a liquid level of the crystallizer 4 from a circulating inlet K1 to realize boiling ward off, along with continuous separation of water vapor from the material, sodium sulfate gradually saturates and crystallizes, the whole flow field of the material in the crystallizer 4 is from top to bottom, the crystallized sodium sulfate has relatively high density, and is continuously deposited downwards into a elutriation cylinder at the bottom along the flow direction, the solid content of the crude sodium sulfate after elutriation is 20+/-5 wt%, the high-concentration organic liquid carried on the surface of particles is replaced by newly-fed low-concentration reducing wastewater, the crystal slurry is pumped out from a crystal slurry side wall outlet K4 and a crystal slurry bottom outlet K5 by a discharging pump B4, the impurity amount of discharged salt is reduced to the greatest extent, and the quality of discharged salt is ensured.
Along with the continuous separation of water vapor from materials, the organic concentration of easy discoloration is also gradually increased, the lower part of the crystallizer 4 is provided with an annular interlayer, the top of the interlayer is provided with a concentrated solution outlet k6, the circumference of the interlayer can be uniformly distributed with multiple points, the concentrated organic concentrated solution in the system is pumped out from the concentrated solution outlet k6 by a concentrated solution pump B3, the flow of the concentrated solution pump B3 is far less than the circulating flow of a circulating pump B2, thereby forming a precipitation standing area with low rising flow velocity in the interlayer, and the concentrated solution outlet k6 is discharged as high-concentration organic concentrated solution without sodium sulfate solids. The high-concentration organic liquid discharged from the crystallizer 4 enters a degumming kettle 12 to be stirred and reacted with 0.3 percent by weight of degumming agent for 4 to 6 hours, organic matters in the high-concentration organic liquid react with the degumming agent to form sludge solids, organic matter slurry enters a degumming centrifuge 13 to be separated, about 350kg of organic solids are produced by the high-concentration organic concentrated liquid of 5m, and the organic matter slurry is discharged from a solid phase of the degumming centrifuge 13.
The organic matter content in the degummed clear liquid can be reduced by about 90%, the degummed clear liquid enters the mother liquid tank 16 for temporary storage, and is sent into the circulating pipe of the crystallizer 4 by the mother liquid pump B5 to return to the crystallizer 4 for recrystallization. Intermittent discharging and degumming in the crystallizer can keep the content of organic matters stable and does not influence the quality of crystallized salt.
And (3) feeding sodium sulfate crystal slurry discharged by the discharge pump B4 into the thickener 14 for thickening and concentrating to 35-45%, feeding clear liquid separated by the crystal slurry centrifugal machine 15 into the mother liquid tank 16 for temporary storage, and feeding the clear liquid back into the crystallizer 4 for recrystallization by the mother liquid pump B5.
The wet salt separated by the crystal slurry centrifugal machine 15 is conveyed into a drying bed 18 through a screw conveyor 17 to be dried by hot air, the dried hot air is sent into high-temperature air at 120 ℃ generated by a fin heat exchanger 20 from a blower 19, and sodium sulfate produced after drying can be sold independently after meeting the requirements of class II first-class products of industrial salt GBT6009-2014, so that the resource utilization of waste salt is realized.
The exhaust air of the drying bed 18 firstly enters the cyclone dust collector 21 to carry out primary dust removal, then enters the bag dust collector 22 to carry out secondary dust removal, and finally is pumped out by the induced draft fan 23 to be discharged. The sodium sulfate fine particles captured by the cyclone dust collector 21 and the bag dust collector 22 also enter the product.
80-82 ℃ Water vapor evaporated by the crystallizer 4 is discharged from a secondary vapor outlet K7, foam possibly carried in the vapor is blocked and cleaned by a secondary separator 6, the leaching water discharged from the bottom of the secondary separator 6 contains a small amount of sodium sulfate and flows back to the crystallizer 4 again, clean secondary vapor enters a primary vapor compressor 7 and a secondary vapor compressor 8 to be subjected to two-stage compression and temperature rise to 100-102 ℃, enters the shell pass of the heater 5 again and is used as a heat source to exchange heat with materials in the tube pass of the heater 5, condensate generated by the vapor enters a condensate tank 9 to be collected, and is sent to a hot side of the condensate water preheater 3 to preheat low-temperature feed and then is discharged out of the system, so that heat recovery is realized to the greatest extent, and the aim of energy conservation is achieved.
A small amount of steam condensate water can be injected into the outlet steam of the primary steam compressor 7 and the secondary steam compressor 8 through the condensate water pipe G3 so as to adjust the steam temperature and improve the steam enthalpy value.
The noncondensable gas discharged from the shell side of the heater 5 enters the surface cooler 10 through the noncondensable gas pipe G4 to be condensed, and is then pumped out by the vacuum pump group 11.
The foregoing description of the preferred embodiments of the present utility model illustrates and describes the basic principles, main features and advantages of the present utility model, and is not intended to limit the scope of the present utility model, as it should be understood by those skilled in the art that the present utility model is not limited to the above-described embodiments. In addition to the embodiments described above, other embodiments of the utility model are possible without departing from the spirit and scope of the utility model. The utility model also has various changes and improvements, and all technical schemes formed by adopting equivalent substitution or equivalent transformation fall within the protection scope of the utility model. The scope of the utility model is defined by the appended claims and equivalents thereof. The technical features of the present utility model that are not described may be implemented by or using the prior art, and are not described herein.
Claims (4)
1. The sodium sulfate wastewater separation and refining system comprises a feeding blending tank and a crystallizer, and is characterized in that a cone hopper is arranged at the lower part of a barrel of the crystallizer, an upper port of the cone hopper is sleeved on the periphery of the barrel to form an annular interlayer, a concentrated solution outlet is arranged on the side wall of the annular interlayer, and a washing barrel is connected with the lower end of the cone hopper;
The outlet of the reducing agent and the pH regulator is connected to a feeding blending tank, the outlet of the feeding blending tank is connected with the cold side inlet of a condensate preheater through a feeding pump, the cold side outlet of the condensate preheater is connected with a elutriation port on the side wall of the elutriation cylinder, the crystal slurry outlet on the lower part of the elutriation cylinder is connected with the inlet of a thickener through a discharging pump, the underflow outlet of the thickener is connected with the inlet of a crystal slurry centrifuge, and the solid phase outlet of the crystal slurry centrifuge is connected with a drying bed through a screw conveyor;
The concentrated solution outlet of the crystallizer is connected with the inlet of the degumming kettle through a concentrated solution pump, the bottom outlet of the degumming kettle is connected with the inlet of a degumming centrifuge, and the liquid phase outlet of the degumming centrifuge is connected with a mother solution tank;
The liquid phase outlet of the crystal slurry centrifugal machine is connected with the overflow port of the thickener respectively with the inlet of the mother liquor tank, the outlet of the mother liquor tank is connected with the circulating pipe of the crystallizer through the mother liquor pump, the circulating pipe of the crystallizer is connected with the pipe side inlet of the heater through the circulating pump, and the pipe side outlet of the heater is connected with the circulating inlet of the crystallizer.
2. The sodium sulfate wastewater separation and purification system containing organic matters easy to change according to claim 1, wherein the system comprises: the secondary steam outlet at the top of the crystallizer is connected with the inlet of the primary steam compressor through the secondary separator, the outlet of the primary steam compressor is connected with the inlet of the secondary steam compressor, the outlet of the secondary steam compressor is connected with the shell side inlet of the heater, the shell side outlet of the heater is connected with the inlet of the condensate water tank, and the outlet of the condensate water tank is connected with the hot side inlet of the condensate water preheater through the condensate water pump.
3. The sodium sulfate wastewater separation and purification system containing organic matters easy to change according to claim 2, wherein: and condensed water injection ports are respectively arranged at the outlets of the primary vapor compressor and the secondary vapor compressor.
4. The sodium sulfate wastewater separation and purification system containing organic matters easy to change according to claim 2, wherein: the shell side inlet of the heater is also connected with a steam generating pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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