CN211620232U - Evaporation system and wastewater treatment system - Google Patents
Evaporation system and wastewater treatment system Download PDFInfo
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- CN211620232U CN211620232U CN201922123216.8U CN201922123216U CN211620232U CN 211620232 U CN211620232 U CN 211620232U CN 201922123216 U CN201922123216 U CN 201922123216U CN 211620232 U CN211620232 U CN 211620232U
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- 238000001704 evaporation Methods 0.000 title claims abstract description 74
- 230000008020 evaporation Effects 0.000 title claims abstract description 57
- 238000004065 wastewater treatment Methods 0.000 title claims description 13
- 238000010438 heat treatment Methods 0.000 claims abstract description 66
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- 239000012528 membrane Substances 0.000 claims description 84
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- 238000001914 filtration Methods 0.000 claims description 40
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model discloses an evaporation system and effluent disposal system, including at least one evaporimeter jar body, set up vacuum port, thermometer mouth, first manometer mouth, feed inlet and discharge gate on the jar body, set up heating device outside jar body. The utility model discloses an evaporation system uses the thermometer of thermometer mouth and the manometer of first manometer mouth to carry out real time monitoring to the temperature and the pressure of the internal liquid of evaporimeter, prevents that the internal portion of evaporating pot from reaching metallic compound's crystallization condition and making metallic compound appear, prevents that the pipeline from blockking up, and whole journey can not appear the solid matter. The utility model discloses do not adopt external heat exchanger to carry out the circulation heating to the internal liquid of jar, but set up the heating jacket in horizontal jar external portion and directly heat jar body itself, the internal liquid of indirect heating jar, temperature control is more accurate, therefore effectively avoids the crystal blockage at the inside liquid of evaporimeter.
Description
Technical Field
The utility model relates to a surface treatment trade waste water treatment field, especially an evaporation system and effluent disposal system.
Background
The surface treatment process refers to a process for decorating and protecting metal or nonmetal surfaces and acquiring certain new surface characteristics by using a chemical or electrochemical method, wherein the components of wastewater discharged in the processes of pre-plating treatment, metal layer plating, post-plating treatment and the like are complex, main pollutants are pollutants of various heavy metals, acid and alkali, surfactants, additives and organic matters, harmful heavy metals are used as the main pollutants, and some Cu is used as the main pollutant2+、Zn2+、Cr3+、Ni2+In the form of iso-cations, some are CrO4 2-、Cr2O7 2-、Cu(CN)4 3-、Cu(P2O7)2 6-In the form of plasma or complex ions. Heavy metals cannot be decomposed and can only be converted into their physical and chemical forms. If the treatment is improper, the heavy metal ions enter the environment by taking soil or water as a medium, which brings great harm to the environment and human health, for example, heavy metal accumulation of crops caused by heavy metal pollution of soil in certain areas; discharge of cyanide-containing waste water into rivers and lakes causes yield reduction and even mass death of fishery and the like.
At present, the treatment of waste water in the surface treatment industry is mainly that various waste water is treated according to the classification of chromium series, cyanogen series, acid-base, oil, phosphorus and the like, and then is comprehensively treated. The method has the advantages of complex flow, multiple operation links, high labor intensity, high operating cost and large amount of generated sludge. The most common method for chromium-series waste water is chemical reduction precipitation method, the basic principle of said method is that waste iron filings or ferrous sulfate are used as reducing agent, firstly, the hexavalent chromium is reduced into trivalent chromium, then the flocculating agent is added to make the trivalent chromium produce hydroxide precipitation, then the solid-liquid separation is implemented so as to attain the goal of removing chromium.
For example, Chinese patent ZL201710983122.0 discloses a method for treating chromium-containing wastewater by a chemical precipitation method and a membrane method, which comprises the steps of rinsing, chemical precipitation, reverse osmosis advanced treatment, evaporation crystallization and the like, wherein hexavalent chromium needs to be reduced to trivalent chromium in the chemical precipitation step, and chemical reduction precipitation is adoptedThe method is characterized in that chromium ions are removed in the step, and the subsequent steps of reverse osmosis advanced treatment, evaporative crystallization and the like are only the treatment of the supernatant after precipitation, namely the treatment of other soluble salts, organic matters, colloids and microorganisms in the supernatant, so that the supernatant reaches the discharge standard, the solid sludge containing chromium obtained by chemical reduction precipitation treatment cannot be reused and can only be discarded or buried, but chromium ion reversion can occur possibly, so that the treatment is abandoned completely, and even more serious pollution is caused by diffusion. In addition, after the chemical precipitation step, hexavalent chromium ions in the waste water are removed, and the salt content in the waste water is greatly increased, such as by using a sulfur dioxide reduction method, SO42-Can remain in the waste water in a large number, when the evaporation step, the waste water is slightly heated, and salinity is a large amount of immediately appearing, blocks up the pipeline of evaporimeter very easily, especially the pipeline of heat exchanger, can only shut down to demolish the washing behind the jam pipeline, seriously influences the treatment process. The prior industrial wastewater evaporation device mostly uses an external heat exchanger to perform cyclic heating, wastewater in the evaporation tank enters the heat exchanger from an external pipeline and is then returned to the evaporation tank through the pipeline, in the step of chemical treatment, the reaction is possibly insufficient, or partial trivalent chromium ions can be reversed, so hexavalent chromium ions can be remained in the wastewater, and because the hexavalent chromium ions have stronger corrosivity, the hexavalent chromium ions can seriously corrode an evaporator tank body in the subsequent evaporation step, so that the evaporator can be damaged and cannot be used.
For example, the prior Chinese patent ZL201110449172.3 discloses a heavy metal wastewater treatment process, wherein wastewater is subjected to oil separation by an oil separation tank and then sequentially enters a comprehensive adjusting tank, a pH adjusting tank, a concentration tank, a tubular ultrafiltration membrane system, a pH adjusting tank and an RO membrane system to finally obtain recycled water, the wastewater containing heavy metals is treated by adopting a physical filtration and pH adjustment mode, a large amount of pH adjusting agents are still required in the treatment process, and the metals, TSS and COD removed by the DF membrane filtration are remained on the DF membrane, when the DF membrane bears a certain pollution amount, the DF membrane must be backwashed or directly discarded, heavy metal wastewater can still be formed during backwashing, and the cost is quite high when the DF membrane is directly discarded, in addition, the method does not treat the residual waste liquid which can not pass through the RO system, the residual waste liquid is still harmful substances which pollute the environment, therefore, the method cannot completely treat the wastewater comprehensively, and a large amount of waste liquid remains after treatment for treatment.
SUMMERY OF THE UTILITY MODEL
The applicant provides an evaporation system and a wastewater treatment system aiming at the defects of easy blockage, high energy consumption and the like of the evaporation system in the existing production, the evaporator is prevented from being blocked, the energy consumption is low, and the mass production is ensured.
The utility model discloses the technical scheme who adopts as follows:
an evaporation system comprises at least one evaporator tank body, a vacuum port, a thermometer port, a first pressure gauge port, a feeding port and a discharging port are formed in the evaporator tank body, and a heating device is arranged outside the evaporator tank body.
As a further improvement of the above technical solution:
the heating device is a heating sleeve sleeved outside the tank body, and a heating medium inlet and a heating medium outlet are formed in the heating sleeve.
The tank body is also provided with a second pressure gauge port and a sewage draining port.
The evaporation system is formed by connecting a plurality of evaporator tanks in parallel.
The tank body is horizontal.
The utility model provides an adopt above-mentioned evaporation system's effluent disposal system, is provided with the export of reuse water on the raw water collecting pit, sand filtration system, precision filtration system, ultrafiltration system, RO membrane system, evaporation system and the roast dry powder system that connects gradually, the roast dry powder system is last to be provided with solid useless export.
As a further improvement of the above technical solution:
still be provided with the ultrafiltration relay jar between ultrafiltration system and the RO membrane system, the RO membrane system is connected with one-level membrane system including a plurality of grades of membrane systems that set gradually, ultrafiltration relay jar, and one-level membrane system's dense solution export is connected with evaporating system, and clear solution relay jar is all connected to the clear solution export of each grade of membrane system, and the dense solution export of each grade of membrane system all is connected with the relay jar in last one-level membrane system the place ahead, and the clear solution exit linkage reuse water of last one-level membrane system exports.
The heating system is respectively connected with the evaporation system and the dry powder baking system, and the heating system is supplied with heat by a gas system.
The cooling system is connected with the RO membrane system; the cooling system and the evaporation system are respectively connected with the condensation system, and a condensed water outlet of the condensation system is connected with the first clear liquid relay tank.
A first concentrated solution relay tank is also arranged between the RO membrane system and the evaporation system.
The utility model has the advantages as follows:
the utility model discloses an evaporation system uses the thermometer of thermometer mouth and the manometer of first manometer mouth to carry out real time monitoring to the temperature and the pressure of the internal liquid of evaporimeter, prevents that the internal portion of evaporating pot from reaching metallic compound's crystallization condition and making metallic compound appear, prevents that the pipeline from blockking up, and whole journey can not appear the solid matter.
The utility model discloses do not adopt external heat exchanger to carry out the circulation heating to the internal liquid of jar, but set up the heating jacket in horizontal jar external portion and directly heat jar body itself, the internal liquid of indirect heating jar, temperature control is more accurate, reduces liquid and takes place to block up when the pipeline, therefore effectively avoids the crystallization of the inside liquid of evaporimeter to block up, more does not have stifled pipe problem.
The waste water treatment system of the utility model does not carry out chemical treatment on chromium oxide, chromic acid glycoside and the like in the waste water in the whole course, and the substances are dissolved in water in a stable compound form, so that the stability is good, and the evaporator can not be corroded; in addition, the crystallization temperature of the compound is far higher than that of a salt substance, so that the compound is not easy to crystallize per se and has certain crystallization resistance, and a pipeline is not easy to block in the evaporation process.
The utility model discloses an evaporation operation method adopts the mode of feeding in batches, evaporating repeatedly, adds new liquid and the concentrated solution that has evaporated once or several times in follow-up step respectively and evaporates together, sets for different temperature and negative pressure condition at different stages, and temperature and pressure rise in proper order, and the concentrated solution is at the internal incessant evaporation that flows of jar, the required energy consumption of saving evaporation that can the at utmost.
The utility model discloses a waste water treatment system is under the condition that heavy metal substance dissolves in water, do not adopt traditional chemical method to add chemical substance and make it deposit and appear, but whole journey adopts physical treatment method, the water-insoluble substance in water is all got rid of earlier, heavy metal compound is extracted out through evaporation, the step of baking, the solid waste that the powder system of baking finally obtained is the compound that contains chromium salt, nickel salt or other metal salts that the purity is very high, these substances can directly repeat and recycle, and need not to bury or abandon the processing, consequently can not produce extra environmental pollution; the utility model adopts a physical treatment mode, does not carry out chemical treatment, saves the chemical treatment step, can save a large amount of chemical reagents, and obviously reduces the production cost; the secondary pollution of chemical reagents in the production process is reduced, and the method is more environment-friendly; can directly recycle heavy metal compounds, and has high economic value.
The utility model discloses set up the secondary filter system before RO membrane filtration system, because oil is very little in the dispersed granule in sewage, be less than the water granule even, this part oil is difficult to float from sewage, if do not get rid of in advance in follow-up RO membrane filtration system, these oily substances block up the RO membrane easily, can get rid of the oily substance in the surface treatment trade waste water through leading secondary filter system, prevent that oily substance from blockking up the RO membrane.
The utility model discloses a set up and just filter, sand filtration, microfiltration, ultrafiltration get rid of large granule, organic matter, oily material and the micro-particle more than 0.5~5um in the waste water in proper order, the micro-particle more than 0.01um, get rid of totally insoluble material in the waste water basically to follow-up RO membrane filters and goes on smoothly.
The utility model discloses set up multistage concentrate backward flow in the RO membrane filtration system of a plurality of levels, the concentrate that begins to filter the production from second level membrane system does not directly enter into evaporation system on next step, but the filtration that carries out the last one-level once more in the relay tank in 9 the place ahead of last one-level membrane system that flows back, circulation filtration makes all concentrates all can only be followed one-level membrane system and held back and discharged in the evaporation system on next step to ensure that the concentration of the concentrate that gets into evaporation system is higher, reduce the required energy consumption of evaporation system overall evaporation.
The utility model discloses a backwash system can be according to the automatic back flush work of accomplishing sand filtration system, precise filtration system, ultrafiltration system and RO membrane system's filter core of each system's respective needs, and on the other hand, the clear water that the filter system filtration obtained lets in the sand of this system once more and filters the relay jar in, and the clear water that the filter system filtration obtained is not independently discharged, and unified the entering the utility model discloses an in-system handles, the delivery port of reducing system, the overall structure of simplified system.
The utility model discloses utilize cooling system to carry out cooling to RO membrane system and condensing system, prevent that RO membrane system high temperature from taking place to damage, when condensing system evaporation effect variation, negative pressure system may unable normal work, and condensing system's evaporation condensation effect can be strengthened to cooling system, guarantees that negative pressure system normally works. The utility model discloses a cooling system, evaporating system are connected with condensing system respectively, and condensing system's comdenstion water delivery port is connected with first clear liquid relay tank, and the comdenstion water gets into first clear liquid relay tank and filters and retrieve, the utility model discloses utilize the water filtration system of itself in the system to collect the filtration to the water that condensing system produced, make the water of production in the entire system all discharge from same delivery port after concentrating the filtration, can reduce the drainage export of this system, simplify the pure water and collect work.
Drawings
Fig. 1 is a process flow diagram of the present invention.
Fig. 2 shows an evaporator tank of the evaporation system of the present invention.
Fig. 3 is a left side view of fig. 2 (showing the internal structure).
In the figure: 1. a raw water collecting tank; 2. a raw water relay tank; 3. a sand filtration system; 4. a sand filtration relay tank; 5. a precision filtration system; 6. a precision filtration relay tank; 7. an ultrafiltration system; 8. an ultrafiltration relay tank; 9. a first stage membrane system; 10. a first concentrate relay tank; 11. a first clear liquid relay tank; 12. a secondary membrane system; 13. a second clear liquid relay tank; 14. a tertiary membrane system; 15. a reuse water system; 16. an evaporation system; 17. a baking powder system; 18. a backwashing system; 19. an air compressor; 20. a filter system; 21. a filter element solid waste disposal device; 22. a gas system; 23. a cooling system; 24. a condensing system; 25. a negative pressure system; 26. a recycled oil outlet; 27. a solid waste outlet; 28. an exhaust gas treatment device; 29. a vacuum port; 30. a thermometer port; 31. a second pressure gauge port; 32. a first pressure gauge port; 33. an inspection opening; 34. a feed inlet; 35. a heating medium outlet; 36. a level gauge port; 37. a heating medium inlet; 38. a discharge port; 39. a sewage draining outlet; 40. a tank body; 41. and (4) heating the sleeve.
Detailed Description
The following describes embodiments of the present invention with reference to the drawings.
As shown in figure 1, effluent disposal system including the raw water collecting pit 1, raw water relay tank 2, sand filtration system 3, sand filtration relay tank 4, accurate filtration system 5, accurate filtration relay tank 6, ultrafiltration system 7, ultrafiltration relay tank 8, RO membrane system, first concentrate relay tank 10, evaporating system 16 and the stoving powder system 17 that connect gradually, be provided with retrieval and utilization oil export 26 on the accurate filtration system 5, RO membrane system is connected with reuse water system 15, is provided with solid useless export 27 on the stoving powder system 17. The utility model discloses set up microfiltration system 5 before RO membrane filtration system, because oil is very little in the sewage dispersed granule, be less than the water granule even, this part oil is difficult to float from sewage, if do not get rid of in advance in follow-up RO membrane filtration system, these oily substances block up the RO membrane easily, can get rid of the oily substance in the surface treatment trade waste water through leading microfiltration system 5, prevent that oily substance from blockking up the RO membrane.
The RO membrane system is including a plurality of grades of membrane systems that set gradually, the common tertiary membrane system of this embodiment, ultrafiltration relay jar 8 is connected with one-level membrane system 9, the concentrate export of one-level membrane system 9 is connected with first concentrate relay jar 10, the clear solution export of one-level membrane system 9 has connected gradually first clear solution relay jar 11, second grade membrane system 12, the concentrate export of second grade membrane system 12 is connected with ultrafiltration relay jar 8, the clear solution export of second grade membrane system 12 has connected gradually second clear solution relay jar 13, tertiary membrane system 14, the clear solution exit linkage reuse water system 15 of tertiary membrane system 14, tertiary membrane system 14's concentrate export is connected with first clear solution relay jar 11.
The utility model discloses set up multistage concentrate backward flow in the RO membrane filtration system of a plurality of levels, concentrate that the production was started to filter from second grade membrane system 12 does not directly enter into evaporating system 16 on next step, but the filtration of going on the one-level again in the relay tank in the preceding place ahead of last one-level membrane system that flows back, circulation filtration makes all concentrates all can only be followed one-level membrane system 9 and held back and discharged in evaporating system 16 on next step to ensure that the concentration of the concentrate that gets into evaporating system 16 is higher, reduce the required energy consumption of 16 global evaporation of evaporating system.
The utility model discloses still be provided with backwash system 18, backwash system 18 is connected with the back flush water inlet of sand filtration system 3, accurate filtration system 5, ultrafiltration system 7 and RO membrane system, and the back flush delivery port of sand filtration system 3, accurate filtration system 5, ultrafiltration system 7 and RO membrane system is connected with filter system 20, and filter system 20's clear water export is connected with sand filtration relay tank 4, and filter system 20's sparge water export is connected with the solid useless processing apparatus 21 of filter core.
The sand filtering system 3 automatically carries out back washing operation respectively according to the value measured by the internal pressure controller, the precision filtering system 5 according to the value measured by the pressure controller and the water yield, the ultrafiltration system 7 and the RO membrane system according to the water yield and the conductivity, when in back washing, the air compressor 19 inputs water into the sand filtering system 3, the precise filtering system 5 or the ultrafiltration system 7, water flow backflushs filter elements of the sand washing filtering system 3, the precise filtering system 5 or the ultrafiltration system 7, the washing water enters the filter system 20 for filtering, impurities obtained by filtering of the filter system 20 enter the filter element solid waste disposal device 21 for disposal, the backflushing system 18 is connected with the RO membrane system at the same time, the washing water discharged by the RO membrane system also enters the filter system 20 for filtering, clear water obtained by filtering of the filter system 20 enters the sand filtering relay tank 4 and then enters a subsequent water disposal link. On the one hand, backwash system 18 can be according to the respective needs of every system automatic completion sand filtration system 3, precision filtration system 5, ultrafiltration system 7 and RO membrane system's back flush work of filter core, and on the other hand, filter system 20 filters the clear water that obtains and lets in this system's sand once more and filters relay jar 4 in, and filter system 20 filters the clear water that obtains and does not independently discharge, and the unified entering the utility model discloses an in-system handles, reduces the delivery port of system, simplifies system overall structure.
The utility model discloses still be provided with the system of heating 21, the system of heating 21 is connected with evaporating system 16 and roast dry powder system 17 respectively, and the system of heating 21 is supplied heat by gas system 22 to provide evaporating system 16 and roast dry powder system 17 with the heat simultaneously. The dry powder baking system 17 is connected with the exhaust gas treatment device 28, and exhaust gas generated in the drying process is treated by the exhaust gas treatment device 28 and then discharged.
The utility model discloses still be provided with cooling system 23, cooling system 23 and RO membrane system's primary membrane system 9, secondary membrane system 12 and tertiary membrane system 14 are connected, cooling system 23 cools down the RO membrane system, cooling system 23, evaporating system 16 is connected with condensing system 24 respectively, condensing system 24's comdenstion water delivery port and first clear solution relay tank 11 are connected, take out to condensing system 24 through the moisture in negative pressure system 25 with cooling system 23 and evaporating system 16 in, the comdenstion water flows into first clear solution relay tank 11, and through secondary membrane system 12, tertiary membrane system 14 discharges. The water generated by the condensing system 24 is collected and filtered by using the water filtering system in the system, so that the water generated in the whole system is discharged from the same water outlet after being concentrated and filtered, the drainage outlet of the system can be reduced, and the pure water collection work is simplified.
The evaporation system 16 comprises a plurality of evaporator tank bodies 40 connected in parallel, as shown in fig. 2 and 3, one end of each horizontal evaporator tank body 40 is closed, the other end of each horizontal evaporator tank body is provided with a liquid level meter port 36, a vacuum port 29, a temperature meter port 30, a second pressure meter port 31, a first pressure meter port 32 and a feed port 34 are sequentially arranged above the tank body 40 from left to right near the closed end, a temperature meter of the temperature meter port 30 and a pressure meter of the first pressure meter port 32 monitor the temperature and the pressure of liquid in the tank body 40, and a pressure meter of the second pressure meter port 31 monitors the pressure of a heating medium. The heating jacket 41 is sleeved outside the lower half part in the tank body close to the tank body 40, the heating medium inlet 37 and the heating medium outlet 35 are respectively arranged at the bottom and the upper part of the heating jacket 41, the heating medium can be hot kerosene, steam, water and the like, heating can be more uniform by adopting hot kerosene heating, other heating modes of electrical heating arranged on the periphery of the tank body 40 can be selected, and the heating jacket 41 can be sleeved on the whole tank body 40. An inspection opening 33 is arranged at the junction of the upper part of the heating jacket 41 and the tank 40 and is used for inspecting the evaporation operation in the tank 40. The bottom of the tank 40 is provided with a cylindrical sewage discharge pipeline, the bottom of the sewage discharge pipeline is provided with a sewage discharge outlet 39, and the side surface of the sewage discharge pipeline is provided with a discharge port 38.
The utility model discloses evaporating system 16's evaporation step sets up 4 to 8 evaporation times, confirms temperature, the negative pressure condition in each stage according to the waste liquid type of difference, realizes through following embodiment:
(i) the interior of the tank 40 is not vacuumized, concentrated solution with the solid content of about 5% enters the evaporator tank 40, the heating sleeve 41 heats the tank 40, heating is stopped when the temperature in the tank 40 is 50-90 ℃, the tank 40 starts to be vacuumized, and the vacuum degree is-0.093 to-0.095 MPa;
(ii) at the moment, the water in the liquid in the tank is quickly evaporated under the conditions of high temperature and low pressure, new concentrated liquid is added after the evaporation is carried out for 2 to 7min, the heating sleeve 41 is continuously heated until the temperature in the tank 40 is 50 to 95 ℃, the interior of the tank 40 is vacuumized again, and the vacuum degree is minus 0.095 to minus 0.097 MPa;
(iii) and (3) repeating the step (2) for 2-6 times, wherein the heating temperature of the heating sleeve 41 is increased by 1-5 ℃ each time, and the vacuum degree of the vacuumizing is increased by 0.001 MPa each time when the step is 1-4. In the last 1-2 steps, no new liquid is added, evaporation is completed after the determined concentration is reached, and the solid content of the concentrated solution finally discharged from the evaporation system 16 is 30-40%.
The amount of liquid added in each step of adding new liquid is 10-35% of the amount of liquid added in the first step, and 1/3 of liquid is preferably constantly added in each step.
First embodiment of evaporation operation:
1. when the treated wastewater is chromium-containing wastewater, about 5% of solid content in the filtrate after the RO membrane step enters the first concentrated solution relay tank 10, 150 kg of concentrated solution in the first concentrated solution relay tank 10 enters the evaporator tank 40, at this time, no vacuum pumping is performed in the tank 40, hot oil enters the heating sleeve 41 from the heating medium inlet 37 and leaves from the heating medium outlet 35, the tank 40 is heated by the hot oil in a circulating manner, when the temperature in the tank 40 is monitored by the thermometer at the thermometer port 30 to be 60 ℃, the heating is stopped, the tank 40 starts to be vacuumized, the vacuum degree is-0.094 MPa until the water starts to boil, and after 2-3min, about 65 kg of water is evaporated.
2. And then 50 kg of concentrated solution is added from the first concentrated solution relay tank 10, in the liquid adding process, a part of vacuum degree and pressure are lost inside the tank body 40, the temperature is reduced, the liquid is heated to 62 ℃ by the heating sleeve 41, the tank body 40 is vacuumized again, the vacuum degree is-0.095 MPa, and after 5-6min, the moisture is evaporated to about 50 kg.
3. Then 50 kg of concentrated solution is added from the first concentrated solution relay tank 10, the heating sleeve 41 heats the solution to 64 ℃, the tank body 40 is vacuumized again, the vacuum degree is-0.095 MPa, and after 5-6min, the water is evaporated to about 50 kg.
4. Then 50 kg of concentrated solution is added from the first concentrated solution relay tank 10, the heating sleeve 41 heats the solution to 66 ℃, the tank body 40 is vacuumized again, the vacuum degree is-0.095 MPa, and after 5-6min, the water is evaporated to about 40 kg.
5. Then 50 kg of concentrated solution is added from the first concentrated solution relay tank 10, the heating sleeve 41 heats the solution to 68 ℃, the tank body 40 is vacuumized again, the vacuum degree is-0.095 MPa, and after 5-6min, the water content is evaporated to about 35 kg.
6. Then no more concentrated solution is added, the heating sleeve 41 heats the liquid to 69 ℃, the tank 40 is vacuumized again, the vacuum degree is-0.096 MPa, and the moisture is evaporated for about 30 kg after 6-7 min.
7. Then no more concentrated solution is added, the heating sleeve 41 heats the liquid to 70 ℃, the tank 40 is vacuumized again, the vacuum degree is-0.097 MPa, moisture is evaporated for about 25 kg after 6-7min, and finally the solid content of the liquid from the evaporation system 16 is 31.8%.
Example two of the evaporation operation:
1. when the treated wastewater is nickel-containing wastewater, the solid content in the filtrate after the RO membrane step is about 5%, the wastewater enters a first concentrated solution relay tank 10, 150 kg of concentrated solution in the first concentrated solution relay tank 10 enters an evaporator tank 40, at the moment, the interior of the tank 40 is not vacuumized, hot oil enters a heating sleeve 41 from a heating medium inlet 37 and leaves from a heating medium outlet 35, the hot oil circularly heats the tank 40, when a thermometer at a thermometer port 30 monitors that the temperature in the tank 40 is 55 ℃, the heating is stopped, the tank 40 starts to be vacuumized, the vacuum degree is-0.094 MPa until water starts to boil, and after 6-7min, the water is evaporated to about 70 kg.
2. Then 50 kg of concentrated solution is added from the first concentrated solution relay tank 10, the heating sleeve 41 heats the solution to 58 ℃, the tank body 40 is vacuumized again, the vacuum degree is-0.095 MPa, and after 5-6min, the water is evaporated to about 50 kg.
3. Then 50 kg of concentrated solution is added from the first concentrated solution relay tank 10, the heating sleeve 41 heats the solution to 61 ℃, the tank body 40 is vacuumized again, the vacuum degree is-0.095 MPa, and after 5-6min, the water is evaporated to about 50 kg.
4. Then 50 kg of concentrated solution is added from the first concentrated solution relay tank 10, the heating sleeve 41 heats the solution to 63 ℃, the tank body 40 is vacuumized again, the vacuum degree is-0.096 MPa, and after 5-6min, the water content is evaporated to about 45 kg.
5. Then 50 kg of concentrated solution is added from the first concentrated solution relay tank 10, the heating sleeve 41 heats the solution to 65 ℃, the tank body 40 is vacuumized again, the vacuum degree is-0.096 MPa, and after 5-6min, the water content is evaporated to about 45 kg.
6. Then no more concentrated solution is added, the heating sleeve 41 heats the liquid to 70 ℃, the tank 40 is vacuumized again, the vacuum degree is-0.097 MPa, moisture is evaporated for about 35 kg after 6-7min, and finally the solid content of the concentrated solution from the evaporation system 16 is 31.8%.
The concentrated solution from the evaporation system 16 is sprayed and dried in the baking powder system 17, and all water is baked out, and finally solid substances are formed.
The wastewater treatment method comprises the following steps:
(I) primary filtration: the method comprises the following steps that wastewater enters a raw water collecting tank 1 for pretreatment, different treatment methods are set according to different wastewater types, large granular substances, suspended particles and organic matters in the wastewater are preliminarily filtered, and the wastewater enters a raw water relay tank 2;
(II) sand filtration: the wastewater enters a sand filtering system 3, organic matters in the wastewater are filtered and removed, the COD value (chemical oxygen demand) in the water is further reduced, gravel is further removed at the same time, and the filtrate enters a sand filtering relay tank 4;
(III) microfiltration: the filtrate enters a precise filtering system 5, oil substances and micro particles above 0.5-5 um in the water are filtered and removed, the filtered oil is discharged from a recycled oil outlet 26, and the filtrate enters a precise filtering relay tank 6;
(IV) ultrafiltration: the filtrate enters an ultrafiltration system 7, and is filtered to remove micro particles above 0.01um, all microorganisms such as bacteria in the water can be removed basically in the step, and the filtrate enters an ultrafiltration relay tank 8;
(V) RO membrane concentration: the filtrate enters a plurality of stages of RO membrane systems, the filter residue which can not pass through the primary membrane system 9 is the heavy metal-containing concentrated solution, the concentrated solution directly enters the first concentrated solution relay tank 10, the clear solution enters the first clear solution relay tank 11, then the clear solution enters the secondary membrane system 12 for secondary membrane filtration, the concentrated solution obtained by the secondary membrane filtration flows back to the ultrafiltration relay tank 8 for the primary membrane system 9 filtration again, the clear solution obtained by the secondary membrane filtration enters the second clear solution relay tank 13, then the clear solution enters the tertiary membrane system 14 for the tertiary membrane filtration, the concentrated solution obtained by the tertiary membrane filtration flows back to the first clear solution relay tank 11 for the secondary membrane filtration again, the clear solution obtained by the secondary membrane filtration, namely the clean recovered water finally obtained, directly enters the reuse water system 15, and the conductivity of the recovered water is below 200 s/m.
(VI) evaporating: the heavy metal-containing concentrated solution in the first concentrated solution relay tank 10 enters an evaporation system 16 and is evaporated by adopting the evaporation method;
(VII) baking dry powder: the evaporated concentrated solution enters a baking powder system 17, a high-purity compound containing chromium salt, nickel salt or other metal salt is obtained by spraying and drying at 250-320 ℃, and is discharged from a solid waste outlet 27, and waste gas generated in the baking process is discharged from a waste gas treatment device 28.
The utility model adopts a physical treatment mode, does not carry out chemical treatment, and the solid waste finally obtained by the baking powder system 17 is a compound containing chromium salt, nickel salt or other metal salts with high purity, and the substances can be directly and repeatedly reused without landfill or discarding treatment, so that no extra environmental pollution is generated, and the utility model has obvious economic value; the method saves the chemical treatment step, also can save a large amount of chemical reagents, avoids secondary pollution of the chemical reagents and obviously reduces the production cost.
The above description is illustrative of the present invention and is not intended to limit the present invention, and the present invention may be modified in any manner without departing from the spirit of the present invention.
Claims (10)
1. An evaporation system, characterized by: the evaporation system (16) comprises at least one evaporator tank body (40), a vacuum port (29), a thermometer port (30), a first pressure gauge port (32), a feeding port (34) and a discharging port (38) are formed in the tank body (40), and a heating device is arranged outside the tank body (40).
2. The vaporization system of claim 1, wherein: the heating device is a heating sleeve (41) sleeved outside the tank body (40), and a heating medium inlet (37) and a heating medium outlet (35) are arranged on the heating sleeve (41).
3. The vaporization system of claim 1, wherein: the tank body (40) is also provided with a second pressure gauge port (31) and a sewage draining port (39).
4. The vaporization system of claim 1, wherein: the evaporation system (16) is formed by connecting a plurality of evaporator tanks (40) in parallel.
5. The vaporization system of claim 1, wherein: the tank body (40) is horizontal.
6. A wastewater treatment system employing the evaporation system of claim 1, wherein: the device comprises a raw water collecting tank (1), a sand filtering system (3), a precise filtering system (5), an ultrafiltration system (7), an RO membrane system, an evaporation system (16) and a baking powder system (17) which are sequentially connected, wherein a reuse water outlet is formed in the RO membrane system, and a solid waste outlet (27) is formed in the baking powder system (17).
7. The wastewater treatment system according to claim 6, characterized in that: still be provided with ultrafiltration relay jar (8) between ultrafiltration system (7) and the RO membrane system, the RO membrane system is including a plurality of levels of membrane systems that set gradually, and ultrafiltration relay jar (8) are connected with one-level membrane system (9), and the concentrate export of one-level membrane system (9) is connected with vaporization system (16), and the clear liquid relay jar is all connected to the clear liquid export of each level of membrane system, and the concentrate export of each level of membrane system all is connected with the relay jar in last one-level membrane system the place ahead, and the clear liquid exit linkage reuse water export of last one-level membrane system.
8. The wastewater treatment system according to claim 6, characterized in that: the heating system (21) is respectively connected with the evaporation system (16) and the dry powder baking system (17), and the heating system (21) is supplied with heat by the gas system (22).
9. The wastewater treatment system according to claim 6, characterized in that: the cooling system (23) is connected with the RO membrane system; the cooling system (23) and the evaporation system (16) are respectively connected with the condensing system (24), and a condensed water outlet of the condensing system (24) is connected with the first clear liquid relay tank (11).
10. The wastewater treatment system according to claim 6, characterized in that: a first concentrated solution relay tank (10) is also arranged between the RO membrane system and the evaporation system (16).
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| Application Number | Priority Date | Filing Date | Title |
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| CN201922123216.8U CN211620232U (en) | 2019-12-02 | 2019-12-02 | Evaporation system and wastewater treatment system |
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|---|---|---|---|
| CN201922123216.8U CN211620232U (en) | 2019-12-02 | 2019-12-02 | Evaporation system and wastewater treatment system |
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