CN112047411A - MVR evaporation crystallization process for sodium sulfate wastewater treatment - Google Patents
MVR evaporation crystallization process for sodium sulfate wastewater treatment Download PDFInfo
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- CN112047411A CN112047411A CN202010977693.5A CN202010977693A CN112047411A CN 112047411 A CN112047411 A CN 112047411A CN 202010977693 A CN202010977693 A CN 202010977693A CN 112047411 A CN112047411 A CN 112047411A
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- heat exchanger
- sodium sulfate
- forced circulation
- separator
- mvr
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/101—Sulfur compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
Abstract
The invention discloses an MVR evaporative crystallization process for treating sodium sulfate wastewater, which comprises the steps of pumping raw materials into a plate heat exchanger through a feed pump, carrying out evaporative concentration through a forced circulation evaporator, carrying out flash evaporation concentration in a crystallization separator, carrying out vapor-liquid separation on concentrated solution and secondary steam in the crystallization separator, heating the generated concentrated solution through the forced circulation heat exchanger, then feeding the heated concentrated solution into the separator for flash evaporation concentration, circulating in the way, feeding the obtained product into a centrifuge for centrifugation after the discharged concentration is reached, feeding the centrifuged crystal into a subsequent treatment system, returning mother liquor to the system for continuous evaporative concentration in the centrifugation process, discharging part of high-boiling mother liquor, discharging 90 ℃ secondary steam from the separator, feeding the obtained product into an MVR compression system, pumping the compressed steam into the forced circulation heat exchanger for heating the materials, and achieving the thermal balance of the whole system. According to the invention, the sodium sulfate wastewater is treated by the MVR evaporative crystallization process, so that the treatment effect of the sodium sulfate wastewater is better, the equipment is simpler, and the operation is more convenient.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to an MVR evaporation crystallization process for treating sodium sulfate wastewater.
Background
A large amount of sodium sulfate wastewater can be generated in the industries of desulfurization, chemical metallurgy, environmental protection and the like, and the wastewater containing sodium sulfate can cause serious pollution after being discharged into a water body, so that the water body is acidified, the pH is reduced, and aquatic organisms are damaged; meanwhile, the sulfate reducing bacteria in the water body can convert SO 42-into toxic gas H2S and even sulfide with stronger toxicity and the like under the anaerobic condition, SO that the human health and the ecological balance of the water body are directly harmed; the soil discharged into farmland can destroy the soil structure, harden the soil, reduce the crop yield and reduce the quality of agricultural products; when the concentration of sodium sulfate in drinking water is as high as 1000mg/L, the sodium sulfate inhibits secretion of gastric juice, and the decrease in the concentration of gastric juice causes decrease in pepsin activity, which hinders digestion.
The contradiction between the development of the world economy and the explosion of population, limited energy and unlimited use is increasingly prominent, and the energy problem becomes the focus of the contradiction of the world economy, and for China, along with the high-speed development of economy, the energy problem becomes more prominent and becomes a road barricade for economic development, and particularly in the industry of sodium sulfate wastewater treatment, the energy consumed by evaporating a large amount of wastewater is the important cost in the sodium sulfate wastewater treatment.
Disclosure of Invention
The invention aims to provide an MVR evaporation crystallization process for treating sodium sulfate wastewater, so as to solve the problems in the background technology.
In order to achieve the purpose, the invention provides the following technical scheme: an MVR evaporation crystallization process for treating sodium sulfate wastewater comprises the following steps:
step S1: feeding, namely pumping the solution to be treated from the raw liquid tank into a plate heat exchanger by a feeding pump, carrying out heat exchange between the feeding liquid and steam condensate water in the plate heat exchanger, preheating by a fresh steam plate, raising the temperature to an evaporation temperature, and then feeding into a forced circulation evaporator for evaporation concentration;
step S2: flash evaporation concentration, wherein the materials enter a forced circulation heat exchanger to be heated and pressurized, then flash evaporation concentration is carried out in a crystallization separator, and the concentrated solution and secondary steam are subjected to vapor-liquid separation in the crystallization separator;
step S3: circulating flash evaporation concentration, pumping the concentrated solution after gas-liquid separation into a forced circulation heat exchanger by a forced circulation pump, continuously heating the concentrated solution in a forced circulation evaporator, then feeding the concentrated solution into a separator, performing flash evaporation concentration in the separator, circulating the steps in the way, and pumping the concentrated solution to a thickener after the discharged material concentration is reached;
step S4: centrifuging, namely, allowing the material in the thickener to enter a centrifuge for centrifugation after thickening, allowing the centrifuged crystal to enter a subsequent treatment system, heating the mother liquor cooled in the centrifuging process to reach an evaporation temperature, returning to the system for continuous evaporation and concentration, and discharging part of high-boiling mother liquor;
step S5: MVR compression, wherein 90 ℃ secondary steam from a separator enters an MVR compression system, the temperature of the compressed secondary steam can be raised to about 104 ℃, the compressed steam is pumped into a forced circulation heat exchanger to heat materials, in the process of heating the materials, the steam with the temperature of about 104 ℃ is condensed into water flow, the water flow flows into a condensate tank and is pumped into a plate heat exchanger by a distilled water pump to exchange heat with raw material liquid, and the water flow is discharged out of the system after the temperature is reduced to about 35 ℃;
step S6: and (3) performing heat exchange evaporation, namely performing heat exchange evaporation on the preheated material after entering an evaporator and the compressed steam which is raised to 104 ℃, so that the whole system achieves heat balance.
Further, the forced circulation heat exchanger in the step S5 is the forced circulation heat exchanger in the step S2.
Further, the raw material in the step S6 is the solution to be processed coming out of the raw material tank in the step S1.
Further, in the steps S1 to S6, the entire evaporation system is controlled by PLC software, and all the output and input signals and the operation of the system can be completed by a computer.
Further, in the steps from S1 to S6, heat preservation measures are arranged on the heat exchanger, the separator and the pipeline, and composite silicate and aluminum skin are wrapped outside the heat preservation measures.
Further, in steps S1 to S6, the specification of the forced circulation heat exchanger is as follows: 300 square meters and diameter: 1000mm, height: 8000 mm.
Further, in the steps S1 to S6, the power cabinet and the frequency conversion cabinet are installed in a matched manner.
Further, in steps S1 to S6, the specifications of the thickener and the mother liquor tank are, diameter: 1400mm, height: 1500 mm.
Compared with the prior art, the invention has the beneficial effects that:
1. according to the invention, the sodium sulfate wastewater is treated by the MVR evaporative crystallization process, so that the treatment effect of the sodium sulfate wastewater is better, the equipment is simpler, and the operation is more convenient;
2. according to the invention, the 90 ℃ secondary steam from the separator enters the MVR compression system, the temperature of the compressed secondary steam can be raised to about 104 ℃, the compressed steam is pumped into the forced circulation heat exchanger to heat materials, in the process of heating the materials, the steam with the temperature of about 104 ℃ is condensed into water flow, the water flow flows into the condensate tank and is pumped into the plate heat exchanger by the distilled water pump to exchange heat with the raw material liquid, the temperature is reduced to about 35 ℃ and is discharged out of the system, the waste heat is effectively utilized, and the energy is saved.
Drawings
FIG. 1 is a schematic view of the overall flow of an MVR evaporative crystallization process for sodium sulfate wastewater treatment according to the present invention;
FIG. 2 is a schematic diagram of water quality analysis data of an MVR evaporative crystallization process for sodium sulfate wastewater treatment according to the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Referring to fig. 1-2, the present invention provides a technical solution: an MVR evaporation crystallization process for treating sodium sulfate wastewater comprises the following steps:
step S1: feeding, namely pumping the solution to be treated from the raw liquid tank into a plate heat exchanger by a feeding pump, carrying out heat exchange between the feeding liquid and steam condensate water in the plate heat exchanger, preheating by a fresh steam plate, raising the temperature to an evaporation temperature, and then feeding into a forced circulation evaporator for evaporation concentration;
step S2: flash evaporation concentration, wherein the materials enter a forced circulation heat exchanger to be heated and pressurized, then flash evaporation concentration is carried out in a crystallization separator, and the concentrated solution and secondary steam are subjected to vapor-liquid separation in the crystallization separator;
step S3: circulating flash evaporation concentration, pumping the concentrated solution after gas-liquid separation into a forced circulation heat exchanger by a forced circulation pump, continuously heating the concentrated solution in a forced circulation evaporator, then feeding the concentrated solution into a separator, performing flash evaporation concentration in the separator, circulating the steps in the way, and pumping the concentrated solution to a thickener after the discharged material concentration is reached;
step S4: centrifuging, namely, allowing the material in the thickener to enter a centrifuge for centrifugation after thickening, allowing the centrifuged crystal to enter a subsequent treatment system, heating the mother liquor cooled in the centrifuging process to reach an evaporation temperature, returning to the system for continuous evaporation and concentration, and discharging part of high-boiling mother liquor;
step S5: MVR compression, wherein 90 ℃ secondary steam from a separator enters an MVR compression system, the temperature of the compressed secondary steam can be raised to about 104 ℃, the compressed steam is pumped into a forced circulation heat exchanger to heat materials, in the process of heating the materials, the steam with the temperature of about 104 ℃ is condensed into water flow, the water flow flows into a condensate tank and is pumped into a plate heat exchanger by a distilled water pump to exchange heat with raw material liquid, and the water flow is discharged out of the system after the temperature is reduced to about 35 ℃;
step S6: and (3) performing heat exchange evaporation, namely performing heat exchange evaporation on the preheated material after entering an evaporator and the compressed steam which is raised to 104 ℃, so that the whole system achieves heat balance.
The forced circulation heat exchanger in the step S5 is the forced circulation heat exchanger in the step S2;
the raw material in the step S6 is the solution to be treated which is discharged from the raw material tank in the step S1;
in the steps S1 to S6, the whole set of evaporation system is controlled by PLC software, all output and input signals and the operation of the system can be completed by a matched computer;
in steps S1 to S6, heat preservation measures are arranged on the heat exchanger, the separator and the pipeline, and composite silicate is adopted for heat preservation, and aluminum skins are wrapped outside the heat exchanger, the separator and the pipeline;
in steps S1 to S6 of the present invention, the specification of the forced circulation heat exchanger is as follows: 300 square meters and diameter: 1000mm, height: 8000 mm;
in the steps S1 to S6, corresponding power cabinets and frequency conversion cabinets are arranged in a matched manner;
in steps S1 to S6 of the present invention, the specifications of the thickener and the mother liquor tank are, diameter: 1400mm, height: 1500 mm.
The working principle is as follows: when the invention is used, the solution to be processed is discharged from a stock solution tank, the solution is pumped into a plate heat exchanger by a feed pump, the feed solution in the plate heat exchanger exchanges heat with steam condensate water, the steam condensate water is preheated by a fresh steam plate and heated to the evaporation temperature, then enters a forced circulation evaporator for evaporation concentration, the material is heated and pressurized in the forced circulation heat exchanger, then is subjected to flash evaporation concentration in a crystallization separator, the concentrated solution and secondary steam are subjected to steam-liquid separation in the crystallization separator, the concentrated solution after the gas-liquid separation is pumped into the forced circulation heat exchanger by a forced circulation pump, the concentrated solution is continuously heated in the forced circulation evaporator, then enters the separator for flash evaporation concentration, the mixture is circulated in the way, the discharged material is pumped into a thickener after reaching the discharge concentration, the material in the thickener enters a centrifuge for centrifugation after being thickened, and the centrifuged crystals enter a subsequent processing system, the mother liquor cooled in the centrifugal process reaches the evaporating temperature after being heated and returns to the system for continuous evaporation and concentration, part of high-boiling mother liquor is discharged outside, 90 ℃ secondary steam discharged from the separator enters the MVR compression system, the temperature of the compressed secondary steam can rise to about 104 ℃, the compressed steam is pumped into a forced circulation heat exchanger to heat materials, in the process of heating the materials, the part of steam with the temperature of about 104 ℃ is condensed into water flow to a condensate tank and pumped into a plate heat exchanger by a distilled water pump to exchange heat with raw material liquid, the temperature is reduced to about 35 ℃ and discharged out of the system, the preheated materials enter an evaporator and then exchange heat with the steam which rises to 104 ℃ after being compressed to evaporate, the whole system reaches the thermal balance, sodium sulfate wastewater is treated by the MVR evaporation and crystallization process, the treatment effect of the sodium sulfate wastewater is better, the equipment is simpler, and the operation is more convenient, and more energy is saved.
It is noted that, herein, relational terms such as first and second, and the like may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (8)
1. An MVR evaporation crystallization process for treating sodium sulfate wastewater is characterized by comprising the following steps:
step S1: feeding, namely pumping the solution to be treated from the raw liquid tank into a plate heat exchanger by a feeding pump, carrying out heat exchange between the feeding liquid and steam condensate water in the plate heat exchanger, preheating by a fresh steam plate, raising the temperature to an evaporation temperature, and then feeding into a forced circulation evaporator for evaporation concentration;
step S2: flash evaporation concentration, wherein the materials enter a forced circulation heat exchanger to be heated and pressurized, then flash evaporation concentration is carried out in a crystallization separator, and the concentrated solution and secondary steam are subjected to vapor-liquid separation in the crystallization separator;
step S3: circulating flash evaporation concentration, pumping the concentrated solution after gas-liquid separation into a forced circulation heat exchanger by a forced circulation pump, continuously heating the concentrated solution in a forced circulation evaporator, then feeding the concentrated solution into a separator, performing flash evaporation concentration in the separator, circulating the steps in the way, and pumping the concentrated solution to a thickener after the discharged material concentration is reached;
step S4: centrifuging, namely, allowing the material in the thickener to enter a centrifuge for centrifugation after thickening, allowing the centrifuged crystal to enter a subsequent treatment system, heating the mother liquor cooled in the centrifuging process to reach an evaporation temperature, returning to the system for continuous evaporation and concentration, and discharging part of high-boiling mother liquor;
step S5: MVR compression, wherein 90 ℃ secondary steam from a separator enters an MVR compression system, the temperature of the compressed secondary steam can be raised to about 104 ℃, the compressed steam is pumped into a forced circulation heat exchanger to heat materials, in the process of heating the materials, the steam with the temperature of about 104 ℃ is condensed into water flow, the water flow flows into a condensate tank and is pumped into a plate heat exchanger by a distilled water pump to exchange heat with raw material liquid, and the water flow is discharged out of the system after the temperature is reduced to about 35 ℃;
step S6: and (3) performing heat exchange evaporation, namely performing heat exchange evaporation on the preheated material after entering an evaporator and the compressed steam which is raised to 104 ℃, so that the whole system achieves heat balance.
2. The MVR evaporative crystallization process for sodium sulfate wastewater treatment according to claim 1, characterized in that: the forced circulation heat exchanger in the step S5 is the forced circulation heat exchanger in the step S2.
3. The MVR evaporative crystallization process for sodium sulfate wastewater treatment according to claim 1, characterized in that: the raw material in the step S6 is the solution to be processed which is discharged from the raw material tank in the step S1.
4. The MVR evaporative crystallization process for sodium sulfate wastewater treatment according to claim 1, characterized in that: in the steps S1 to S6, the entire evaporation system is controlled by PLC software, and all the output and input signals and the operation of the system can be completed by a computer.
5. The MVR evaporative crystallization process for sodium sulfate wastewater treatment according to claim 1, characterized in that: in the steps S1 to S6, heat preservation measures are arranged on the heat exchanger, the separator and the pipeline, and the heat preservation adopts composite silicate and is wrapped by aluminum skin.
6. The MVR evaporative crystallization process for sodium sulfate wastewater treatment according to claim 1, characterized in that: in steps S1 to S6, the specification of the forced circulation heat exchanger is as follows: 300 square meters and diameter: 1000mm, height: 8000 mm.
7. The MVR evaporative crystallization process for sodium sulfate wastewater treatment according to claim 1, characterized in that: and in the steps S1 to S6, corresponding power cabinets and frequency conversion cabinets are installed in a matched manner.
8. The MVR evaporative crystallization process for sodium sulfate wastewater treatment according to claim 1, characterized in that: in the steps S1 to S6, the specifications of the thickener and the mother liquor tank are both, diameter: 1400mm, height: 1500 mm.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202010977693.5A CN112047411A (en) | 2020-09-17 | 2020-09-17 | MVR evaporation crystallization process for sodium sulfate wastewater treatment |
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| CN202010977693.5A CN112047411A (en) | 2020-09-17 | 2020-09-17 | MVR evaporation crystallization process for sodium sulfate wastewater treatment |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114712874A (en) * | 2022-02-25 | 2022-07-08 | 武汉凯迪水务有限公司 | MVR strong brine slurry crystallization salt separation system |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105836951A (en) * | 2016-05-23 | 2016-08-10 | 江苏瑞升华能源科技有限公司 | Treatment process and device of electroplating wastewater |
| CN209507647U (en) * | 2018-10-28 | 2019-10-18 | 江苏长山环保科技有限公司 | A kind of system based on MVR system clean waste water |
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- 2020-09-17 CN CN202010977693.5A patent/CN112047411A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105836951A (en) * | 2016-05-23 | 2016-08-10 | 江苏瑞升华能源科技有限公司 | Treatment process and device of electroplating wastewater |
| CN209507647U (en) * | 2018-10-28 | 2019-10-18 | 江苏长山环保科技有限公司 | A kind of system based on MVR system clean waste water |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114712874A (en) * | 2022-02-25 | 2022-07-08 | 武汉凯迪水务有限公司 | MVR strong brine slurry crystallization salt separation system |
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Application publication date: 20201208 |