CN218011111U - Efficient steam distribution and two-stage compressor series MVR evaporation separation device - Google Patents
Efficient steam distribution and two-stage compressor series MVR evaporation separation device Download PDFInfo
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- CN218011111U CN218011111U CN202222402548.1U CN202222402548U CN218011111U CN 218011111 U CN218011111 U CN 218011111U CN 202222402548 U CN202222402548 U CN 202222402548U CN 218011111 U CN218011111 U CN 218011111U
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Abstract
The utility model relates to the technical field of sewage treatment, in particular to a steam high-efficiency distribution and two-stage compressor series MVR evaporation separation device, which comprises a preheating unit, a low-boiling salt unit crystallized by low-temperature evaporation, a high-boiling salt unit crystallized by high-temperature evaporation, a low-temperature steam compression unit, a high-temperature steam compression unit and a condensed water unit; through adopting the technique of the high-efficient energy-conserving mechanical steam recompressor series connection of two-stage, effectively distribute the heat transfer difference in temperature, realize the high-efficient utilization of steam, the energy consumption that 1t water was produced to the vaporization system is about 1/6 to 1/5 of traditional evaporimeter, outside steam use amount is few, reduce the reliance to steam equipment such as boilers, the service limit of traditional MVR system has been expanded, the emission of pollutant has been reduced, it is more energy-concerving and environment-protective, the device process flow is simple, and easy to realize, degree of automation is high, the running cost is low, accord with sustainable development requirement, but wide application in the actual industrial production process.
Description
Technical Field
The utility model relates to a sewage treatment technical field, specific is a high-efficient distribution of steam, two-stage compressor series connection MVR evaporation and separation device.
Background
In recent years, environmental and energy problems have become the most prominent problems affecting the long-term stable development of countries and enterprises, along with the rapid development of industry, the variety and quantity of waste water are rapidly increased, the pollution to water is more and more extensive and serious, and the health and safety of human beings are threatened.
The hazards of industrial wastewater are mainly: heavy metals and other toxic and harmful substances which are difficult to degrade enter soil along with sewage and are continuously enriched, so that the heavy metals in the farmland exceed the standard and the food safety is harmed; the sludge of the sewage treatment plant is influenced by industrial sewage, the harmful substances exceed the standard, and the sludge cannot be used as fertilizer to return to the land, so that the circulation of substances such as nitrogen, phosphorus and the like is influenced; the industrial wastewater is recycled as soon as possible under the large environment that water resource saving utilization and environmental protection are greatly promoted in China, and zero emission refers to that the wastewater, waste liquid and waste residues generated in the production process of enterprises are recycled and reused without any discharge.
In the zero discharge process of industrial wastewater in the industries of salt chemical industry, chlor-alkali chemical industry, coal chemical industry, wet smelting, pharmacy and the like, the wastewater simultaneously contains low-boiling salt, high-boiling salt and high COD components, if the wastewater is directly evaporated and crystallized, the gradual enrichment of the high-boiling components in the evaporation concentration process can greatly increase the burden of an evaporation system, and when a large amount of concentrated solution is discharged to cause environmental pollution, the treatment energy consumption can be increased by independent treatment, the treatment cost is high, and the economic type is poor.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a steam high-efficient distribution, two-stage compressor series MVR evaporation and separation device to solve the problem that provides among the above-mentioned background art.
The purpose of the utility model can be realized by the following technical scheme:
a vapor efficient distribution and two-stage compressor series MVR evaporation separation device comprises a preheating unit, a low-boiling-point salt unit obtained by low-temperature evaporation and crystallization, a high-boiling-point salt unit obtained by high-temperature evaporation and crystallization, a low-temperature vapor compression unit, a high-temperature vapor compression unit and a condensed water unit;
the preheating unit is communicated with the low-boiling-point salt evaporation and crystallization unit, the preheating unit is communicated with the condensed water unit, the high-boiling-point salt evaporation and crystallization unit is communicated with the low-temperature steam compression unit, the low-boiling-point salt evaporation and crystallization unit is communicated with the high-temperature steam compression unit, the high-temperature steam compression unit is communicated with the low-temperature steam compression unit, and the condensed water unit is communicated with the high-boiling-point salt evaporation and crystallization unit and the low-temperature salt evaporation and crystallization unit.
Preferably, the preheating unit comprises a raw material tank, a feed pump, a condensate water preheater, a noncondensable gas preheater and a fresh steam preheater which are sequentially communicated.
Preferably, the condensed water unit comprises a condensed water tank and a condensed water pump, the condensed water tank is communicated with the condensed water pump, the preheating unit and the condensed water unit are communicated with a condensed water preheater through the condensed water pump, and the condensed water tank is communicated with the fresh steam preheater.
Preferably, the low-temperature vapor compression unit comprises a low-temperature vapor compressor, a low-temperature secondary separator and a low-temperature forced circulation heat exchanger which are sequentially communicated, and the low-temperature forced circulation heat exchanger is communicated with the condensed water tank;
preferably, the high-temperature vapor compression unit comprises a high-temperature vapor compressor, a high-temperature forced circulation heat exchanger and a high-temperature secondary separator, the high-temperature vapor compressor is communicated with the high-temperature forced circulation heat exchanger, the high-temperature vapor compressor and the high-temperature forced circulation heat exchanger are both communicated with the high-temperature secondary separator, the low-temperature forced circulation heat exchanger is communicated with the high-temperature forced circulation heat exchanger, and the low-temperature secondary separator is communicated with the high-temperature vapor compressor.
Preferably, the low-boiling-salt evaporation and crystallization unit comprises a low-temperature forced circulation heat exchanger, a low-temperature forced circulation pump, a low-temperature crystallization separator, a low-temperature discharge pump, a low-boiling-salt thickener, a low-boiling-salt centrifuge, a low-boiling-salt mother liquor tank and a low-boiling-salt mother liquor pump which are sequentially communicated;
the low-boiling-point salt mother liquor pump is communicated with the low-temperature forced circulation pump, the fresh steam preheater is communicated with the low-temperature crystallization separator, the non-condensable gas preheater is communicated with the low-temperature crystallization separator, the low-temperature secondary separator is communicated with the low-temperature crystallization separator, the low-boiling-point salt thickener is communicated with the low-boiling-point salt mother liquor tank, the low-temperature forced circulation heat exchanger is communicated with the low-temperature crystallization separator, and the low-temperature crystallization separator is communicated with the high-temperature steam compressor.
Preferably, the high-temperature evaporation crystallization high-boiling salt discharging unit comprises a high-temperature forced circulation heat exchanger, a high-temperature forced circulation pump, a high-temperature crystallization separator, a high-temperature discharging pump, a high-boiling salt thickener, a high-boiling salt centrifuge, a high-boiling salt mother liquor tank and a high-boiling salt mother liquor pump which are sequentially communicated;
the high-boiling-salt mother liquor pump and the high-temperature crystallization separator are communicated with a high-temperature forced circulation pump, the high-temperature secondary separator is communicated with the high-temperature crystallization separator, the high-temperature forced circulation heat exchanger is communicated with the high-temperature crystallization separator, the low-temperature crystallization separator is communicated with the high-temperature forced circulation heat exchanger, a low-boiling-salt transfer pump is communicated between the low-temperature forced circulation pump and the high-temperature crystallization separator, and the high-boiling-salt thickener is communicated with the high-boiling-salt mother liquor tank.
Preferably, the low-boiling-point salt evaporation and crystallization unit at low temperature and the high-boiling-point salt evaporation and crystallization unit at high temperature further comprise a vacuum control system, the vacuum control system comprises a vacuum pump cooler, the vacuum pump cooler is communicated with a vacuum pump for controlling the vacuum degree, and the vacuum pump cooler is communicated with the noncondensable gas preheater.
The utility model has the advantages that:
through low temperature evaporative crystallization material liquid evaporative concentration or crystallization in low boiling point district is matchd to low boiling point salt unit, high temperature evaporative crystallization material liquid evaporative concentration or crystallization in high boiling point district is matchd to high boiling point salt unit, thereby realized the function of the high-efficient distribution of boiling point and steam when low concentration and high concentration of material, the expansion breaks through the barrier of traditional MVR mechanical type vapor compression system processing low boiling point material, compare environmental protection and energy saving more when high boiling point material uses multiple effect evaporation system simultaneously.
Through adopting the technique of two-stage high-efficient energy-conserving mechanical vapor recompressor series connection, effectively distribute the heat transfer difference in temperature, realize the high-efficient utilization of steam, the energy consumption that evaporation system produced 1t water is about 1/6 to 1/5 of traditional evaporimeter, outside steam use amount is few, reduce the reliance to steam equipment such as boilers, the service boundary of traditional MVR system has been expanded, the emission of pollutant has been reduced, it is more energy-concerving and environment-protective, the device process flow is simple, easily realize, degree of automation is high, the running cost is low, accord with sustainable development requirement, but wide application in actual industrial production process.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without creative efforts;
fig. 1 is a schematic view of the overall structure of the present invention.
The reference numbers in the figures are as follows:
1. vacuum pump, 2, raw material tank, 3, vacuum pump cooler, 4, charge pump, 5, condensed water preheater, 6, noncondensable gas preheater, 7, fresh steam preheater, 8, low-temperature steam compressor, 9, condensed water pump, 10, low-temperature secondary separator, 11, condensed water tank, 12, low-temperature forced circulation heat exchanger, 13, low-temperature crystallization separator, 15, low-temperature forced circulation pump, 16, high-temperature steam compressor, 17, low-temperature discharge pump, 18, low-boiling salt mother liquor pump, 19, low-boiling salt transfer pump, 20, low-boiling salt mother liquor tank, 21, low-boiling salt centrifuge, 22, low-boiling salt thickener, 23, high-temperature forced circulation heat exchanger, 24, high-temperature secondary separator, 25, high-temperature forced circulation pump, 26, high-temperature crystallization separator, 27, high-boiling salt mother liquor pump, 28, high-temperature discharge pump, 29, high-boiling salt mother liquor tank, 30, high-boiling salt, 31, high-boiling salt thickener.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by a person of ordinary skill in the art without creative efforts belong to the protection scope of the present invention.
A vapor efficient distribution and two-stage compressor series MVR evaporation separation device comprises a preheating unit, a low-boiling-point salt unit obtained by low-temperature evaporation and crystallization, a high-boiling-point salt unit obtained by high-temperature evaporation and crystallization, a low-temperature vapor compression unit, a high-temperature vapor compression unit and a condensed water unit;
the preheating unit is communicated with the low-boiling-point salt evaporation and crystallization unit, the preheating unit is communicated with the condensed water unit, the high-boiling-point salt evaporation and crystallization unit is communicated with the low-temperature steam compression unit, the low-boiling-point salt evaporation and crystallization unit is communicated with the high-temperature steam compression unit, the high-temperature steam compression unit is communicated with the low-temperature steam compression unit, and the condensed water unit is communicated with the high-boiling-point salt evaporation and crystallization unit and the low-temperature salt evaporation and crystallization unit.
The preheating unit comprises a raw material tank 2, a feeding pump 4, a condensate water preheater 5, a noncondensable gas preheater 6 and a fresh steam preheater 7 which are sequentially communicated.
As shown in figure 1, the fresh steam preheater 7 is communicated with a low-temperature crystallization separator 13 in a low-temperature evaporation crystallization low-boiling salt unit; the evaporation temperature of the high-boiling salt unit obtained by high-temperature evaporation crystallization is 75-85 ℃, the secondary steam is compressed by a high-temperature steam compressor 16, then is heated and pressurized to 85-95 ℃, then enters a low-temperature steam compressor 8 for compression, is heated and pressurized to 95-105 ℃, and then enters a high-temperature forced circulation heat exchanger 23.
The fresh steam pressure in the fresh steam preheater 7 is 195KPa and the temperature is 120 ℃.
The condensate water unit comprises a condensate water tank 11 and a condensate water pump 9, the condensate water tank 11 is communicated with the condensate water pump 9, the preheating unit and the condensate water unit are communicated with a condensate water preheater 5 through the condensate water pump 9, and the condensate water tank 11 is communicated with a fresh steam preheater 7.
The low-temperature vapor compression unit comprises a low-temperature vapor compressor 8, a low-temperature secondary separator 10 and a low-temperature forced circulation heat exchanger 12 which are sequentially communicated, wherein the low-temperature forced circulation heat exchanger 12 is communicated with a condensate water tank 11;
the high-temperature vapor compression unit comprises a high-temperature vapor compressor 16, a high-temperature forced circulation heat exchanger 23 and a high-temperature secondary separator 24, wherein the high-temperature vapor compressor 16 is communicated with the high-temperature forced circulation heat exchanger 23, the high-temperature vapor compressor 16 and the high-temperature forced circulation heat exchanger 23 are both communicated with the high-temperature secondary separator 24, the low-temperature forced circulation heat exchanger 12 is communicated with the high-temperature forced circulation heat exchanger 23, and the low-temperature secondary separator 10 is communicated with the high-temperature vapor compressor 16.
The low-temperature evaporation crystallization low-boiling salt discharging unit comprises a low-temperature forced circulation heat exchanger 12, a low-temperature forced circulation pump 15, a low-temperature crystallization separator 13, a low-temperature discharging pump 17, a low-boiling salt thickener 22, a low-boiling salt centrifuge 21, a low-boiling salt mother liquor tank 20 and a low-boiling salt mother liquor pump 18 which are sequentially communicated;
the low-boiling-point salt mother liquor pump 18 is communicated with the low-temperature forced circulation pump 15, the fresh steam preheater 7 is communicated with the low-temperature crystallization separator 13, the non-condensable gas preheater 6 is communicated with the low-temperature crystallization separator 13, the low-temperature secondary separator 10 is communicated with the low-temperature crystallization separator 13, the low-boiling-point salt thickener 22 is communicated with the low-boiling-point salt mother liquor tank 20, the low-temperature forced circulation heat exchanger 12 is communicated with the low-temperature crystallization separator 13, and the low-temperature crystallization separator 13 is communicated with the high-temperature steam compressor 16.
The high-temperature evaporation crystallization high-boiling salt discharging unit comprises a high-temperature forced circulation heat exchanger 23, a high-temperature forced circulation pump 25, a high-temperature crystallization separator 26, a high-temperature discharging pump 28, a high-boiling salt thickener 31, a high-boiling salt centrifuge 30, a high-boiling salt mother liquor tank 29 and a high-boiling salt mother liquor pump 27 which are sequentially communicated;
the high-boiling-salt mother liquor pump 27 and the high-temperature crystallization separator 26 are communicated with a high-temperature forced circulation pump 25, the high-temperature secondary separator 24 is communicated with the high-temperature crystallization separator 26, the high-temperature forced circulation heat exchanger 23 is communicated with the high-temperature crystallization separator 26, the low-temperature crystallization separator 13 is communicated with the high-temperature forced circulation heat exchanger 23, the low-boiling-salt material transfer pump 19 is communicated between the low-temperature forced circulation pump 15 and the high-temperature crystallization separator 26, and the high-boiling-salt thickener 31 is communicated with the high-boiling-salt mother liquor tank 29.
The low-boiling-point salt unit obtained by low-temperature evaporation and crystallization and the high-boiling-point salt unit obtained by high-temperature evaporation and crystallization further comprise a vacuum control system, the vacuum control system comprises a vacuum pump cooler 3, the vacuum pump cooler 3 is communicated with a vacuum pump 1 used for controlling the vacuum degree, and the vacuum pump cooler 3 is communicated with a noncondensable gas preheater 6.
For the treatment of a sodium sulfate-sodium nitrate solution with a sodium sulfate mass fraction of 15% and a sodium nitrate mass fraction flow of 2%,20t/h, the operating parameters are shown in table 1:
TABLE 1 operating parameters
| Name of material | Sodium chloride sodium sulfate solution |
| Sodium sulfate content (%) | 15 |
| Sodium nitrate content (%) | 2 |
| Sodium sulfate Evaporation temperature (. Degree.C.) | 90 |
| Evaporation temperature (. Degree.C.) of sodium nitrate | 75 |
| Total amount of stock solution (T/h) | 20 |
| Evaporation capacity (T/h) | 16.4 |
Foretell a high-efficient distribution of vapour, two-stage compressor series connection MVR evaporation separator adopt energy-efficient two-stage mechanical vapor recompression technique, and the thermal efficiency is high, and the low power dissipation adopts mechanical vapor recompression technique, uses less bright steam heating, has reduced the reliance to boiler equipment, has reduced the pollutant, and is pollution-free to the environment, more energy-concerving and environment-protective, the utility model discloses an adopt low temperature evaporation crystallization low boiling salt and high temperature evaporation crystallization high boiling salt to broken through one-stage compressor compression temperature and risen low, be difficult to handle the difficulty of high boiling point material, reduced the outer discharge of high concentration material simultaneously, reduce the pollutant, reduce treatment cost.
The utility model provides a pair of high-efficient distribution of steam, two-stage compressor series MVR evaporation and separation device's theory of operation as follows:
in the embodiment, the efficient steam distribution and two-stage compressor series MVR evaporation separation device is suitable for treating 20t/h sodium sulfate and sodium nitrate solution with the treatment temperature of 98 ℃, the mass fraction of sodium sulfate of 15 percent, the mass fraction of sodium nitrate of 2 percent.
Wherein, as shown in fig. 1, preheat the unit including the head tank 2 that communicates in proper order, charge pump 4, condensate water pre-heater 5, noncondensable gas pre-heater 6 and fresh steam pre-heater 7, fresh steam pre-heater 7 and low-temperature crystallization separator 13 intercommunication, sodium sulfate sodium nitrate solution of pending is stored in head tank 2, through charge pump 4 effect, get into condensate water pre-heater 5 in proper order, noncondensable gas pre-heater 6 and fresh steam pre-heater 7, with the distilled water in condensate water pre-heater 5, noncondensable gas in noncondensable gas pre-heater 6 and the fresh steam in the fresh steam pre-heater 7 carry out the heat transfer, make the head tank temperature reach 98 ℃, wherein, fresh steam's pressure is 198KPa in the fresh steam pre-heater 7, the temperature is 120 ℃, condensate water pre-heater 5, noncondensable gas pre-heater 6 and fresh steam pre-heater 7 are plate preheater, condensate water pre-heater 5 has a condensate water pitcher 11 through condensate water pump 9 intercommunication, condensate water pitcher 11 still communicates with fresh steam pre-heater 7 through the pipeline.
Sodium sulfate and sodium nitrate solution with the temperature of 95 ℃ enters a low-temperature crystallization separator 13, then sequentially enters a low-temperature forced circulation pump 15 and a low-temperature forced circulation heat exchanger 12, is subjected to flash evaporation separation after being heated and pressurized, and enters the low-temperature crystallization separator 13, wherein the evaporation temperature in the low-temperature crystallization separator 13 is 90 ℃ and the pressure in the low-temperature crystallization separator is 70.1KPa; and pumping the concentrated solution subjected to flash separation into a low-temperature forced circulation heat exchanger 12 through a low-temperature forced circulation pump 15 for heating and evaporation again, circulating the concentrated solution, allowing sodium sulfate crystals generated by flash separation to grow crystals and settle in a low-temperature crystallization separator 13, then conveying the crystals into a low-boiling salt thickener 22 from the bottom through a low-temperature discharge pump 17, discharging the crystals after thickening into a low-boiling salt centrifuge 21 for centrifugal separation, separating the sodium sulfate crystals out of the system, conveying the separated mother solution into a low-boiling salt mother solution tank 20, pumping the separated mother solution back into the low-temperature forced circulation heat exchanger through a low-boiling salt mother solution pump 18, and circulating the steps.
And (3) regularly detecting the content of sodium nitrate in the low-boiling-salt mother liquor tank 20, and pumping the sodium nitrate into a high-temperature evaporation and crystallization unit through a low-boiling-salt transfer pump 19 when the content of sodium nitrate reaches about 30%.
The mother liquor enters a high-temperature crystallization separator 26, then sequentially enters a high-temperature forced circulation pump 25 and a high-temperature forced circulation heat exchanger 23, after the temperature and the pressure are raised, the mother liquor enters the high-temperature crystallization separator 26 for flash separation, the evaporation temperature in the high-temperature crystallization separator 26 is 75 ℃, and the pressure is 40.1KPa; the concentrated solution after the flash separation is pumped into a high-temperature forced circulation heat exchanger 23 through a high-temperature forced circulation pump 25 to be heated and evaporated again, the concentrated solution circulates in this way, sodium nitrate crystals generated by the flash separation are fed into a high-boiling salt thickener 31 from the bottom through a high-temperature discharge pump 28 after crystal growth and sedimentation in a high-temperature crystallization separator 26, the crystals are discharged into a high-boiling salt centrifuge 30 after being thickened to be centrifugally separated, the sodium nitrate crystals are separated out and sent out of the system, the separated mother solution enters a high-boiling salt mother solution tank 29 and is pumped back to the low-temperature forced circulation heat exchanger through a high-boiling salt mother solution pump 27, and the circulation is carried out in this way.
The steam compression unit comprises a low-temperature steam compressor 8 and a high-temperature steam compressor 16, wherein the low-temperature steam compressor 8 is communicated with a low-temperature secondary separator 10, and the high-temperature steam compressor 16 is communicated with a high-temperature secondary separator 24.
Condensed water at about 105 ℃ in the shell pass of the high-temperature forced circulation heat exchanger 23 and the low-temperature forced circulation heat exchanger 12 automatically flows to the condensed water tank 11, is sent to the condensed water preheater 5 by the condensed water pump 9 to be fully exchanged with raw material liquid, and is discharged out of the device.
Compared with the prior art, the utility model provides a pair of high-efficient distribution of steam, two-stage compressor series connection MVR evaporation and separation device has following beneficial effect:
through low temperature evaporation crystallization feed liquid evaporative concentration or crystallization in low boiling point district of low boiling salt unit matching, high temperature evaporation crystallization feed liquid evaporative concentration or crystallization in high boiling point district of high boiling salt unit matching, thereby realized the function of the high-efficient distribution of boiling point and steam when low concentration and high concentration of material, the expansion breaks through the barrier of traditional MVR mechanical type vapor compression system processing low boiling point material, environmental protection and energy saving more when comparing high boiling point material and using multi-effect evaporation system simultaneously.
The low-temperature evaporation unit and the high-temperature evaporation unit are not required to be adjusted in concentration times, salt production quality of the low-temperature evaporation unit can be effectively improved, the range of materials treated by the high-temperature evaporation unit is wider, the technical effect of resource recovery of zero-pollution liquid discharge is realized, the energy consumption of the separation process is low, treated wastewater can be recycled, and the method is suitable for industrial treatment of various salt-containing wastewater.
Through adopting the technique of two-stage high-efficient energy-conserving mechanical vapor recompressor series connection, effectively distribute the heat transfer difference in temperature, realize the high-efficient utilization of steam, the energy consumption that evaporation system produced 1t water is about 1/6 to 1/5 of traditional evaporimeter, outside steam use amount is few, reduce the reliance to steam equipment such as boilers, the service boundary of traditional MVR system has been expanded, the emission of pollutant has been reduced, it is more energy-concerving and environment-protective, the device process flow is simple, easily realize, degree of automation is high, the running cost is low, accord with sustainable development requirement, but wide application in actual industrial production process.
The foregoing shows and describes the general principles, essential features, and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the above embodiments, and that the foregoing embodiments and descriptions are provided only to illustrate the principles of the present invention without departing from the spirit and scope of the present invention.
Claims (8)
1. A vapor efficient distribution and two-stage compressor series MVR evaporation separation device is characterized by comprising a preheating unit, a low-boiling-point salt evaporation and crystallization unit at low temperature, a high-boiling-point salt evaporation and crystallization unit at high temperature, a low-temperature vapor compression unit, a high-temperature vapor compression unit and a condensed water unit;
the preheating unit is communicated with the low-boiling-point salt evaporation and crystallization unit, the preheating unit is communicated with the condensed water unit, the high-boiling-point salt evaporation and crystallization unit is communicated with the low-temperature steam compression unit, the low-boiling-point salt evaporation and crystallization unit is communicated with the high-temperature steam compression unit, the high-temperature steam compression unit is communicated with the low-temperature steam compression unit, and the condensed water unit is communicated with the high-boiling-point salt evaporation and crystallization unit and the low-temperature salt evaporation and crystallization unit.
2. The efficient steam distribution and two-stage compressor series MVR evaporation and separation device according to claim 1, wherein the preheating unit comprises a raw material tank (2), a feed pump (4), a condensed water preheater (5), a non-condensable gas preheater (6) and a fresh steam preheater (7) which are communicated in sequence.
3. The efficient steam distribution and two-stage compressor series MVR evaporation separation device according to claim 2, wherein the condensed water unit comprises a condensed water tank (11) and a condensed water pump (9), the condensed water tank (11) is communicated with the condensed water pump (9), the preheating unit and the condensed water unit are communicated with the condensed water preheater (5) through the condensed water pump (9), and the condensed water tank (11) is communicated with the fresh steam preheater (7).
4. The efficient vapor distribution and two-stage compressor series MVR evaporation separation device according to claim 3, wherein the low temperature vapor compression unit comprises a low temperature vapor compressor (8), a low temperature secondary separator (10) and a low temperature forced circulation heat exchanger (12) which are sequentially communicated, and the low temperature forced circulation heat exchanger (12) is communicated with the condensed water tank (11).
5. The efficient vapor distribution and two-stage compressor series MVR evaporation separation device according to claim 4, wherein the high temperature vapor compression unit comprises a high temperature vapor compressor (16), a high temperature forced circulation heat exchanger (23) and a high temperature secondary separator (24), the high temperature vapor compressor (16) is communicated with the high temperature forced circulation heat exchanger (23), the high temperature vapor compressor (16) and the high temperature forced circulation heat exchanger (23) are both communicated with the high temperature secondary separator (24), the low temperature forced circulation heat exchanger (12) is communicated with the high temperature forced circulation heat exchanger (23), and the low temperature secondary separator (10) is communicated with the high temperature vapor compressor (16).
6. The efficient steam distribution and two-stage compressor series MVR evaporation and separation device according to claim 5, wherein the low-temperature evaporation crystallization low-boiling salt unit comprises a low-temperature forced circulation heat exchanger (12), a low-temperature forced circulation pump (15), a low-temperature crystallization separator (13), a low-temperature discharge pump (17), a low-boiling salt thickener (22), a low-boiling salt centrifuge (21), a low-boiling salt mother liquor tank (20) and a low-boiling salt mother liquor pump (18) which are sequentially communicated;
the low-boiling-point salt mother liquor pump (18) is communicated with the low-temperature forced circulation pump (15), the fresh steam preheater (7) is communicated with the low-temperature crystallization separator (13), the non-condensable gas preheater (6) is communicated with the low-temperature crystallization separator (13), the low-temperature secondary separator (10) is communicated with the low-temperature crystallization separator (13), the low-boiling-point salt thickener (22) is communicated with the low-boiling-point salt mother liquor tank (20), the low-temperature forced circulation heat exchanger (12) is communicated with the low-temperature crystallization separator (13), and the low-temperature crystallization separator (13) is communicated with the high-temperature steam compressor (16).
7. The efficient steam distribution and two-stage compressor series MVR evaporation and separation device according to claim 6, wherein the high temperature evaporation crystallization high-boiling salt discharging unit comprises a high temperature forced circulation heat exchanger (23), a high temperature forced circulation pump (25), a high temperature crystallization separator (26), a high temperature discharging pump (28), a high-boiling salt thickener (31), a high-boiling salt centrifuge (30), a high-boiling salt mother liquor tank (29) and a high-boiling salt mother liquor pump (27) which are sequentially communicated;
the high-boiling-salt mother liquor pump (27) and the high-temperature crystallization separator (26) are communicated with a high-temperature forced circulation pump (25), the high-temperature secondary separator (24) is communicated with the high-temperature crystallization separator (26), the high-temperature forced circulation heat exchanger (23) is communicated with the high-temperature crystallization separator (26), the low-temperature crystallization separator (13) is communicated with the high-temperature forced circulation heat exchanger (23), a low-boiling-salt transfer pump (19) is communicated between the low-temperature forced circulation pump (15) and the high-temperature crystallization separator (26), and the high-boiling-salt thickener (31) is communicated with the high-boiling-salt mother liquor tank (29).
8. The efficient steam distribution and two-stage compressor series MVR evaporation separation device according to claim 7, wherein the low-temperature evaporation crystallization low-boiling salt unit and the high-temperature evaporation crystallization high-boiling salt unit further comprise a vacuum control system, the vacuum control system comprises a vacuum pump cooler (3), the vacuum pump cooler (3) is communicated with a vacuum pump (1) for controlling the vacuum degree, and the vacuum pump cooler (3) is communicated with the noncondensable gas preheater (6).
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| CN202222402548.1U CN218011111U (en) | 2022-09-09 | 2022-09-09 | Efficient steam distribution and two-stage compressor series MVR evaporation separation device |
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| CN202222402548.1U CN218011111U (en) | 2022-09-09 | 2022-09-09 | Efficient steam distribution and two-stage compressor series MVR evaporation separation device |
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