CN210764418U - Evaporation crystallization separation integration system - Google Patents
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- CN210764418U CN210764418U CN201921293641.5U CN201921293641U CN210764418U CN 210764418 U CN210764418 U CN 210764418U CN 201921293641 U CN201921293641 U CN 201921293641U CN 210764418 U CN210764418 U CN 210764418U
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Abstract
The utility model discloses an evaporation, crystallization and separation integrated system, which comprises an evaporation system and a crystallization system; the evaporation system comprises a gas-liquid separator, an evaporation heater and a first Roots steam compressor, the gas-liquid separator is provided with a waste liquid inlet, a circulating pump is arranged between the gas-liquid separator and the evaporation heater and used for enabling waste liquid to flow between the gas-liquid separator and the evaporation heater in a circulating mode, a gas outlet of the gas-liquid separator is connected with a gas inlet of the first Roots steam compressor, and a high-temperature high-pressure gas outlet of the first Roots steam compressor is connected with a gas inlet of the evaporation heater. The system collects evaporative concentration and separation crystallization in an organic whole to roots vapor compressor is the heat source main part, and the heat source is self-sufficient, need not heat sources such as plus steam, concentrates the waste liquid earlier, carries out concentration decrement processing back, and rethread crystal system crystallization handles, improves treatment effeciency, reduces the energy consumption, and the mother liquor after the solid-liquid separation enters evaporative crystallizer again and carries out concentrated crystallization, and whole system does not have the waste liquid and discharges.
Description
Technical Field
The utility model relates to a wastewater treatment system, concretely relates to evaporation crystallization separation integration system.
Background
Water pollution is one of the main environmental problems faced by China. With the development of industry, the discharge amount of waste water is increasing day by day, and after the industrial waste water which does not reach the discharge standard is discharged into a water body, surface water and underground water can be polluted. Once the water body is polluted, it is not easy to restore the original state in a short time. After the water body is polluted, the water quality of the water body is not in accordance with the standards of drinking water and fishery water, and chemical harmful substances and hardness in underground water are increased, so that the utilization of the underground water is influenced. Water resources in China are not abundant, and if the water resources are calculated according to the average occupied amount of the population, the water resources are only one fourth of the average value of people in the world. The pollution of surface water and underground water further reduces the quantity of available water resources increasingly, thus tending to influence the industrial, agricultural and fishery production and directly or indirectly bringing harm to the life and physical health of people.
Heavy metal pollution is environmental pollution caused by heavy metals and their compounds. The main sources of the wastewater comprise the following aspects: water discharged during mining of ores and paragenic ores thereof; waste water of metal and alloy smelting process; machining the wastewater; waste liquid discharged during the production of salt and catalyst; waste water discharged from electroplating operation, electrochemical machining, etching and rinsing operation of alloy and stainless steel material, etc.
The current common treatment process technologies for high-concentration heavy metal wastewater include chemical reduction, electrolysis, ion exchange and membrane separation (TFS) treatment.
Chemical reduction method: relevant reagents are put into the wastewater containing heavy metals for chemical reaction, and metal ions and the reagents react to generate a compound for precipitation separation and removal.
An electrolytic method: the electrolysis method is a treatment technology for carrying out migration and adhesion on metal ions in the wastewater through an electric field and a charge potential. The treatment technology is generally only suitable for high-concentration heavy metal wastewater with small water quantity and without other impurity metal ions, and the metal ions in the wastewater are finally recovered by metal sheets. However, for the heavy metal-containing wastewater with low concentration, concentration of only tens or hundreds of ppm, large water amount, low concentration and large concentration change, the electrolysis method is difficult to realize effective migration of metal ions in the wastewater. Moreover, the salt content of the electrolyzed wastewater is greatly increased, and the stable discharge and reuse are difficult to achieve.
Ion exchange method: the ion exchange method generally adsorbs metal ions in the wastewater by an ion exchange resin. The metal ions in the wastewater are adsorbed by the resin, and after a period of time, the resin is saturated and fails, so that a large amount of acid or alkali is consumed for elution and regeneration. The regeneration process requires a large amount of tap water for elution and cleaning, which also contains residual metal ions and needs to be treated before discharge. After the ion exchange resin is repeatedly used, the ion exchange resin fails for a period of time, and the ion exchange resin needs to be entirely replaced after the ion exchange resin fails, so that high treatment cost is caused.
Membrane separation treatment method: the membrane separation method is used for effectively isolating metal ions in the wastewater by a pure physical separation and interception method, and no chemical agent is added in the treatment process of the method for carrying out chemical reaction on the metal ions. Directly isolating and concentrating metal ions in the wastewater.
Each method has the following disadvantages:
the chemical reduction method is controlled by the concentration of inlet water and the addition of chemicals, so that the change is uncontrollable and the like, the outlet water can not be stably discharged up to the standard, and the treated wastewater can not be recycled to the production process; because a large amount of medicament needs to be added to participate in the reaction in the treatment process, the medicament cost is higher; the disposal cost of the sludge reaches thousands yuan per ton, the comprehensive cost is high, the treatment effect is unstable, and the risk of secondary pollution of the sludge is faced.
The electrolysis method has higher requirement on the quality of inlet water, is generally only suitable for high-concentration heavy metal wastewater which has less water quantity and does not contain other impurity metal ions, and is difficult to realize effective migration of metal ions in the wastewater by the electrolysis method for the heavy metal wastewater which has generally low concentration, concentration of dozens or hundreds of ppm, large water quantity, low concentration and large concentration change. Moreover, the salt content of the electrolyzed wastewater is greatly increased, and the stable discharge and reuse are difficult to achieve.
Ion exchange requires extensive acid or base consumption for elution and regeneration. The regeneration process requires a large amount of tap water for elution and cleaning, which also contains residual metal ions and needs to be treated before discharge. After the ion exchange resin is repeatedly used, the ion exchange resin loses efficacy for a period of time, the ion exchange resin needs to be wholly replaced after losing efficacy, and the replaced waste resin needs to be subjected to hazardous waste treatment, so that high treatment cost is caused.
The membrane separation method is used for effectively isolating metal ions in the wastewater by a pure physical separation and interception method, and no chemical agent is added in the treatment process of the method for carrying out chemical reaction on the metal ions. Directly isolating and concentrating metal ions in the wastewater. In recent years, the membrane separation method, the membrane separation and evaporation concentration combined process are widely applied to the treatment of heavy metal wastewater. However, since the concentrated solution cannot be directly reused or crystallized due to the limitation of the concentration ratio, a high-concentration concentrated solution of a certain ratio still remains, and thus it is necessary to remove the concentrated solution.
Disclosure of Invention
The utility model aims to overcome the weak point that prior art exists and provide an evaporation crystallization separation integration system.
In order to achieve the above purpose, the utility model adopts the following technical scheme: an evaporation, crystallization and separation integrated system comprises an evaporation system and a crystallization system;
the evaporation system comprises a gas-liquid separator, an evaporation heater and a first Roots steam compressor, the gas-liquid separator is provided with a waste liquid inlet, a circulating pump is arranged between the gas-liquid separator and the evaporation heater and used for enabling waste liquid to circularly flow between the gas-liquid separator and the evaporation heater, a gas outlet of the gas-liquid separator is connected with a gas inlet of the first Roots steam compressor, and a high-temperature and high-pressure gas outlet of the first Roots steam compressor is connected with a gas inlet of the evaporation heater;
the crystallization system comprises an evaporative crystallizer; a finished liquid outlet in the gas-liquid separator is connected with the evaporative crystallizer; the discharge port of the evaporation crystallizer is connected with a crystallization-promoting tank, the discharge port of the crystallization-promoting tank is connected with a solid-liquid separator, and a liquid outlet of the solid-liquid separator is connected with the evaporation crystallizer; a stirring device is arranged in the evaporation crystallizer; the evaporation crystallizer is connected with the second Roots vapor compressor.
And a circulating pump is arranged between the gas-liquid separator and the evaporation heater, waste liquid to be treated is pumped to the evaporation heater from the gas-liquid separator through the circulating pump, and then is circulated back to the circulation inlet of the gas-liquid separator, so that the waste liquid is circularly heated and evaporated and concentrated. And the vapor outlet of the first Roots vapor compressor and high-temperature and high-pressure gas exchange heat and increase the temperature in the evaporation heater. And the secondary steam evaporated by the gas-liquid separator enters an air inlet of the first Roots steam compressor to be compressed, heated and pressurized to form high-pressure and high-temperature gas. The first Roots vapor compressor is used as a heat source, exchanges heat with materials in the evaporation heater, and circularly heats, evaporates and concentrates through the circulating pump, and discharges to the crystallization system after reaching the concentration requirement.
Evaporative crystallization separation integration system collection evaporative concentration and separation crystallization in an organic whole to roots vapor compressor is the heat source main part, and the heat source is self-sufficient, need not heat sources such as plus steam, completion liquid outlet among the vapour and liquid separator is saturated or supersaturated (contains a small amount of crystallization) waste liquid, carries out concentrated decrement processing back with the waste liquid earlier, and rethread crystallization system crystallization handles, improves the treatment effeciency, reduces the energy consumption, be equipped with agitating unit in the evaporative crystallizer, the difficult scale deposit of evaporative crystallization process to improve heat exchange efficiency. The mother liquor after solid-liquid separation is fed into the evaporative crystallizer again for concentration and crystallization, and the whole system has no waste liquid discharge.
Preferably, the evaporation system further comprises a plate heat exchanger, a liquid inlet of the plate heat exchanger is connected with the waste liquid to be treated, a liquid outlet of the plate heat exchanger is connected with a waste liquid inlet of the gas-liquid separator, and a condensate outlet of the evaporation heater is connected with the plate heat exchanger. And the condensate of the evaporation heater exchanges heat with the waste liquid to be treated and is used for preheating the waste liquid to be treated.
High temperature, the high pressure saturated steam that first roots vapor compressor came out form low temperature low pressure steam or comdenstion water behind the heat transfer with the waste liquid in the evaporation heater, get into plate heat exchanger and carry out the heat transfer with the waste liquid of pending, preheat the intensification to the material, and the concentration efficiency in the follow-up vapour and liquid separator can be improved to the maximum utilization waste heat, the energy saving. The plate heat exchanger can be provided with one or more stages according to requirements.
Preferably, the air inlet and the air outlet of the first roots vapor compressor are respectively provided with a temperature transmitter and a pressure transmitter for detecting the temperature and the pressure of the steam of the air inlet and the air outlet, the frequency of the first roots vapor compressor is adjusted at any time through the PLC control system, and the normal operation of the system in the design range is ensured.
Preferably, the evaporation system further comprises a waste liquid storage tank, and a preheater is arranged in the waste liquid storage tank. The preheater is used for heating the waste liquid to be treated before the gas-liquid separator is started, and can be closed after the gas-liquid separator is started, and the plate heat exchanger is used for preheating the waste liquid.
Preferably, the liquid outlet of the plate heat exchanger is connected with a waste liquid storage tank. The liquid outlet of the plate heat exchanger is respectively connected with a waste liquid inlet of the gas-liquid separator and a waste liquid storage tank.
Preferably, the evaporation heater is a shell and tube heat exchanger.
Preferably, the crystallization system further comprises a transfer tank; a finished liquid outlet in the gas-liquid separator is connected with the evaporative crystallizer through a transfer storage tank; and a liquid outlet of the solid-liquid separator is connected with the evaporative crystallizer through a transfer storage tank.
Preferably, a heat-preserving jacket and a stirrer are arranged on the crystallization-assisting tank, and cooling liquid is arranged in the heat-preserving jacket. And the crystallization assisting groove is used for cooling and crystallizing the waste liquid concentrated from the evaporation crystallizer.
Preferably, the waste liquid is high-concentration heavy metal waste liquid.
Preferably, the evaporation, crystallization and separation integrated system further comprises a box body, and the evaporation system and the crystallization system are both arranged in the box body. Evaporation crystallization separation integration system's simple structure, rationally distributed, convenient operation, it is little to take up an area of the space, can all locate a box with all devices in, as portable container formula, can effectively satisfy requirements such as the daily, emergency treatment of high concentration waste liquid of factory enterprise.
The beneficial effects of the utility model reside in that: the utility model provides an evaporative crystallization separation integration system, the system collects evaporative concentration and separation crystallization in an organic whole to roots vapor compressor is the heat source main part, and the heat source is self-sufficient, need not heat sources such as plus steam, concentrates the waste liquid to saturated or supersaturated (contain a small amount of crystallization) waste liquid earlier, carries out concentration decrement processing back, and rethread crystallization system crystallization handles, improves the treatment effeciency, reduces the energy consumption, and the mother liquor after the solid-liquid separation enters evaporative crystallizer again and carries out the concentrated crystallization, and whole system does not have the waste liquid and discharges.
Drawings
FIG. 1 is a schematic diagram of an evaporation system;
FIG. 2 is a schematic diagram of the structure of a crystallization system;
wherein, 1, an evaporation system; 2. a crystallization system; 101. a waste liquid storage tank; 102. a liquid separator; 103. an evaporation heater; 104. a first roots vapor compressor; 105. a plate heat exchanger; 106. a circulation pump; 107. a distillate collection tank; 201. a transfer storage tank; 202. an evaporative crystallizer; 203. a second roots vapor compressor; 204. a crystal assisting groove; 205. a vacuum filter tank; 206. a mother liquor tank; 207. a hot water tank.
Detailed Description
For better illustrating the objects, technical solutions and advantages of the present invention, the present invention will be further described with reference to the following embodiments.
Examples
An embodiment of evaporation crystallization separation integration system, the schematic structure of this embodiment is shown in fig. 1 ~ 2, evaporation crystallization separation integration system includes vaporization system 1, crystallization system 2 and box (not shown in the figure), inside 3 boxes are all located to vaporization system 1 and crystallization system 2, and box 3 is 3.0 x 3.3 x 12.0 m's carriage, is the open-type above the carriage.
The evaporation system 1 comprises a waste liquid storage tank 101, a gas-liquid separator 102 (phi 1000mm x 3700mm), an evaporation heater 103 (a shell-and-tube heat exchanger, phi 900 x 6000mm, a double-tube pass), a first roots vapor compressor 104(2000kg/h,132kW) and a plate heat exchanger 105, wherein the volume V of the waste liquid storage tank 101 is 2000L, a liquid outlet of the waste liquid storage tank 101 is connected with liquid inlets of 2 plate heat exchangers 105 connected in series through a feed pump, and the area of each plate heat exchanger 105 is 4m2The liquid outlet of the plate heat exchanger 105 is respectively connected with the waste liquid inlet of the gas-liquid separator 102 and the waste liquid storage tank 101 through a circulating pump;
a circulating pump 106 is arranged between the gas-liquid separator 102 and the evaporation heater, the circulating pump 106 is used for enabling waste liquid to circularly flow between the gas-liquid separator 102 and the evaporation heater 103, a secondary steam outlet of the gas-liquid separator 102 is connected with a gas inlet of the first roots steam compressor 104, and a high-temperature and high-pressure gas outlet of the first roots steam compressor 104 is connected with a gas inlet of the evaporation heater 103; the condensate outlet of the vaporization heater 103 is connected to a plate heat exchanger 105. The condensate of the evaporation heater 103 exchanges heat with the waste liquid to be treated, and is used for preheating the waste liquid to be treated. The condensate outlet of the plate heat exchanger 105 is connected with a distillate collecting tank 107, and the liquid collected by the distillate collecting tank 107 can be conveyed to a reuse point by a drain pump to be used as reuse water or directly discharged for treatment.
A preheater (not shown in the figure) is arranged in the waste liquid storage tank 101, and the preheater is five groups of electric heating rods, each group has 12kW, and is used for preheating the waste liquid before the gas-liquid separator is started.
The air inlet and the air outlet of the first roots vapor compressor 104 are both provided with temperature and pressure transmitters for detecting the vapor temperature and the vapor pressure of the air inlet and the air outlet, and the frequency of the first roots vapor compressor is adjusted at any time through the PLC control system, so that the normal operation of the system in the design range is ensured.
The crystallization system 2 comprises a transfer storage tank 201, an evaporative crystallizer 202, a second Roots vapor compressor 203, a crystallization assisting tank 204, a vacuum filter tank 205 and a mother liquor tank 206; the finished liquid outlet of the gas-liquid separator 102 is connected with a transfer storage tank 201, and the volume of the transfer storage tank 201 is 2m3(ii) a The transfer storage tank 201 is connected with the evaporative crystallizer 202 through a feed pump, the size of the evaporative crystallizer 202 is phi 1400mm multiplied by 5000mm, the evaporative crystallizer 202 is a shell-and-tube heating device with stirring and vapor-liquid separation equipment, a stirring device and a frequency converter are arranged in the evaporative crystallizer 202, the stirring speed can be adjusted, the lower portion of the evaporative crystallizer is a shell-and-tube heat exchange structure, the upper portion of the evaporative crystallizer is a shell-and-liquid separator tank structure, heating steam walks away from a shell pass, the material infiltrates into the lower portion of the shell-and-tube structure, the material circularly flows in the tube pass through the stirring effect, and the shell-and-tube is provided with. The evaporative crystallizer 202 is connected with a second Roots vapor compressor 203, and the second Roots vapor compressor 203 is 500kg/h and 36 kW; the discharge port of the evaporative crystallizer 202 is connected with a crystallization-promoting tank 204, the crystallization-promoting tank 204 is provided with a heat-insulating jacket, cooling liquid is arranged in the jacket, and a cooling liquid outlet of the evaporative crystallizer 202 is connected with a hot water tank 207; the size of the crystal assisting groove 204 is phi 1000mm multiplied by 2200 mm; the discharge port of the crystallization-promoting tank 204 is connected with a vacuum filter tank 205 (specification 1300X 1000mm), the liquid outlet of the vacuum filter tank 205 is connected with a mother liquor tank 206 (volume 500L) through a mother liquor circulating pump (not shown in the figure), the mother liquor tank 206 is connected with a transfer storage tank 201 through a circulating pump (not shown in the figure), and the solid in the vacuum filter tank 205 is removed after being collected.
The air inlet and the air outlet of the second roots vapor compressor 203 are both provided with temperature and pressure transmitters for detecting the vapor temperature and the pressure of the air inlet and the air outlet, the frequency of the first roots vapor compressor is adjusted at any time through the PLC control system, and the normal operation of the system in the design range is ensured.
The evaporative crystallizer 202 is a shell-and-tube heating and gas-liquid separating device with stirring, the lower part is of a shell-and-tube heat exchange structure, and the upper part is of a vapor-liquid separator tank body structure. Heating steam flows away from a shell pass, the materials infiltrate a part of shell-and-tube structure, the materials circularly flow in the tube pass under the action of stirring, and the shell-and-tube structure is provided with an intermediate circulating tube for placing a stirring and material circulating channel, and the equipment is a central circulating evaporator.
When the evaporation, crystallization and separation integrated system works, high-concentration heavy metal waste liquid to be treated enters the waste liquid storage tank 101, a preheater in the waste liquid storage tank 101 is started, the gas-liquid separator 102, the evaporation heater 103 and the first roots vapor compressor 104 are started after heating for a period of time, and the preheater is closed. Waste water to be treated enters a two-stage plate heat exchanger 105, the plate heat exchanger 105 is divided into two branches, one branch enters a waste liquid storage tank 101, the other branch enters a gas-liquid separator 102, the flow rate of the waste liquid is regulated through valves respectively, the waste liquid circularly flows under the action of a circulating pump 106 through the gas-liquid separator 102 and an evaporation heater 103, secondary steam separated from the evaporation separator 102 enters a first roots steam compressor 104 for compression and temperature rise, the enthalpy of the secondary steam is improved, and the generated high-temperature high-pressure saturated steam enters the evaporation heater 103 to exchange heat with the waste liquid; the waste liquid is heated and then recycled to the recycling inlet of the gas-liquid separator 102, and is subjected to cyclic heating, evaporation and concentration in the way. High-temperature high-pressure saturated steam from the first roots steam compressor 104 exchanges heat with waste liquid in the evaporation heater to form low-temperature low-pressure steam or condensed water, the low-temperature low-pressure steam or the condensed water is discharged to the two-stage plate heat exchanger 105 to exchange heat with waste water to be treated, the waste heat of the waste water to be treated is heated, the waste heat generated by the system is utilized to the maximum extent, the condensed water after the heat exchange of the two-stage plate heat exchanger 105 is collected to the distillate collecting tank 107, and the condensed water is conveyed to a recycling point by the drainage pump 1 to be used as recycled water or directly. The waste liquid is evaporated in the evaporation system by cyclic heating, and finally evaporated and concentrated until saturated or a small amount of crystals are precipitated (according to specific conditions), and the waste liquid is discharged to the transit storage tank 201 by a discharge pump.
The concentrated waste liquid of transfer storage tank 201 is gone into evaporative crystallizer 202 by the pump, the secondary steam that evaporative crystallizer 202 evaporation came out gets into second roots vapor compressor 203 air inlet, produce for the high pressure behind second roots vapor compressor 203, high temperature saturated steam, the high pressure that comes out from second roots vapor compressor 203, high temperature saturated steam gets into evaporative crystallizer 202's shell side, heat transfer with the material intensifies, the effect of agitator is for preventing the material crystallization and precipitation, improve material fluidity, promote heat exchange efficiency. The material is evaporated and concentrated after reaching the boiling point until crystals are separated out, and is discharged to the crystallization assisting groove 204 after reaching a certain degree to be cooled and crystallized, and is discharged to the crystallization assisting groove 204, the crystallization assisting groove 204 is jacket type equipment and is provided with a circulating cooling water inlet and a stirring device, and the material liquid exchanges heat with cooling circulating water in the crystallization assisting groove 204 to be cooled, so that the material crystal solubility is reduced, and the material solid content is improved. The crystal slurry liquid is discharged to a vacuum filter tank 205 after being cooled by a crystal assisting tank 204. The principle of the vacuum filter tank 205 is that filter cloth or filter bags (small holes are correspondingly arranged at the bottom of the tank) are laid at the bottom of the tank, the tank bottom is reserved with space and is connected with a mother liquor tank, the mother liquor tank is vacuumized under the action of a vacuum pump, and thus solid-liquid separation can be carried out on the crystal slurry liquid. The separated mother liquor is pumped into a transfer storage tank 201 and sent to an evaporative crystallizer 202 for concentration, and dry crystals generated by a vacuum filter 205 are collected. And discharging secondary steam condensate water generated in the evaporative crystallization to a sewage station for treatment and discharge.
The high-temperature high-pressure saturated steam generated by the second roots vapor compressor 203 passes through the evaporative crystallizer 202 to form condensed water, and the condensed water is discharged to the hot water tank 207 for collection and can be pumped to a recycling point by a drainage pump or directly discharged for treatment.
The wastewater to be treated is evaporated and concentrated by an evaporation system 1 to reach a certain concentration (saturated or supersaturated state), and then enters a crystallization system 2 for re-concentration and crystallization. Because the crystallization system 2 is provided with a stirring system, the deposition and scaling of materials can be reduced in the crystallization process, the heat conductivity coefficient of the materials is increased, and the treatment effect is improved. The evaporation system 1 can rapidly process the wastewater to be treated, after the wastewater is concentrated to a certain concentration, the concentration of the wastewater is increased, the temperature rise is increased, the boiling point is increased, the evaporation capacity is reduced, if the wastewater is concentrated to be crystallized all the time, the treatment effect is seriously influenced, and the treatment efficiency is reduced. The two stages of evaporation concentration and evaporation crystallization are adopted to respectively treat the wastewater, so that the wastewater is reduced firstly and then crystallized and separated, the treatment efficiency is improved, and the energy consumption is reduced.
The whole evaporation, crystallization and separation integrated system is simple in structure, reasonable in layout, convenient to operate and small in occupied space, and the evaporation system and the crystallization system are integrally installed in a 3.0 x 3.3 x 12.0m standard carriage and can effectively meet the requirements of daily and emergency treatment of high-concentration waste liquid of factory enterprises as a movable container type. In this example, the amount of waste liquid to be treated in the evaporation system 1 was 2000kg/h, and the amount of waste liquid to be treated in the crystallization system 2 was 500 kg/h.
Finally, it should be noted that the above embodiments are only used for illustrating the technical solutions of the present invention and not for limiting the protection scope of the present invention, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that the technical solutions of the present invention can be modified or replaced with equivalents without departing from the spirit and scope of the technical solutions of the present invention.
Claims (9)
1. An evaporation, crystallization and separation integrated system is characterized by comprising an evaporation system and a crystallization system;
the evaporation system comprises a gas-liquid separator, an evaporation heater and a first Roots steam compressor, the gas-liquid separator is provided with a waste liquid inlet, a circulating pump is arranged between the gas-liquid separator and the evaporation heater and used for enabling waste liquid to circularly flow between the gas-liquid separator and the evaporation heater, a gas outlet of the gas-liquid separator is connected with a gas inlet of the first Roots steam compressor, and a high-temperature and high-pressure gas outlet of the first Roots steam compressor is connected with a gas inlet of the evaporation heater;
the crystallization system comprises an evaporative crystallizer; a finished liquid outlet in the gas-liquid separator is connected with the evaporative crystallizer; the discharge port of the evaporation crystallizer is connected with a crystallization-promoting tank, the discharge port of the crystallization-promoting tank is connected with a solid-liquid separator, and a liquid outlet of the solid-liquid separator is connected with the evaporation crystallizer; a stirring device is arranged in the evaporation crystallizer; the evaporation crystallizer is connected with the second Roots vapor compressor.
2. The integrated evaporative crystallization separation system as claimed in claim 1, wherein the evaporative system further comprises a plate heat exchanger, a liquid inlet of the plate heat exchanger is connected with the waste liquid to be treated, a liquid outlet of the plate heat exchanger is connected with a waste liquid inlet of the gas-liquid separator, and a condensate outlet of the evaporative heater is connected with the plate heat exchanger.
3. The integrated evaporative crystallization separation system of claim 1, further comprising a waste liquid storage tank, wherein a preheater is disposed in the waste liquid storage tank.
4. The integrated evaporative crystallization separation system as claimed in claim 2, wherein the liquid outlet of the plate heat exchanger is further connected to a waste liquid storage tank.
5. The integrated evaporative crystallization separation system of claim 1, wherein the evaporative heater is a shell and tube heat exchanger.
6. The integrated evaporative crystallization separation system of claim 1, wherein the crystallization system further comprises a transfer tank; a finished liquid outlet in the gas-liquid separator is connected with the evaporative crystallizer through a transfer storage tank; and a liquid outlet of the solid-liquid separator is connected with the evaporative crystallizer through a transfer storage tank.
7. An evaporation, crystallization and separation integrated system as claimed in claim 1, wherein the crystallization-promoting tank is provided with a heat-insulating jacket and a stirrer, and the heat-insulating jacket is provided with a cooling liquid.
8. The integrated evaporative crystallization separation system of claim 1, wherein the waste stream is a high concentration heavy metal waste stream.
9. An evaporation, crystallization and separation integrated system as claimed in any one of claims 1 to 8, further comprising a box body, wherein the evaporation system and the crystallization system are both arranged in the box body.
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| CN110436546A (en) * | 2019-08-09 | 2019-11-12 | 广州市中绿环保有限公司 | A kind of evaporative crystallization isolation integral system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110436546A (en) * | 2019-08-09 | 2019-11-12 | 广州市中绿环保有限公司 | A kind of evaporative crystallization isolation integral system |
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