CN114772671A - Two-stage MVR single-effect forced circulation evaporation production device and method for salt-containing wastewater - Google Patents
Two-stage MVR single-effect forced circulation evaporation production device and method for salt-containing wastewater Download PDFInfo
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- CN114772671A CN114772671A CN202210666646.8A CN202210666646A CN114772671A CN 114772671 A CN114772671 A CN 114772671A CN 202210666646 A CN202210666646 A CN 202210666646A CN 114772671 A CN114772671 A CN 114772671A
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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
- C02F1/048—Purification of waste water by evaporation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/26—Multiple-effect evaporating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
- B01D1/2896—Control, regulation
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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
Abstract
The invention discloses a two-stage MVR single-effect forced circulation evaporation production device and a method for salt-containing wastewater, wherein the device comprises a raw material tank, a feeding pump, a two-stage preheater, a first-stage heating chamber, a first-stage separation chamber, a first-stage circulating pump, a second-stage heating chamber, a second-stage separation chamber, a second-stage circulating pump, a third-stage heating chamber, a discharging pump, a thickener, a centrifuge and a mother liquor pool which are sequentially connected through pipelines; saturated live steam holding vessel passes through the pipe connection with two-stage preheater, one-level heating chamber, second grade heating chamber and tertiary heating chamber respectively, utilizes the high-energy efficiency steam compressor compression evaporation to produce the flash steam, converts the electric energy into heat energy, improves the enthalpy of flash steam, is squeezed into the evaporating chamber by the flash steam that improves heat energy and heats to reach the existing heat energy of cyclic utilization flash steam, thereby can not need outside steam, realize evaporation concentration's purpose through the evaporimeter self-loopa. The invention has low comprehensive energy consumption and is easy for industrial production.
Description
Technical Field
The invention relates to the technical field of salt-containing wastewater evaporative crystallization, in particular to a double-stage MVR single-effect forced circulation evaporative production device and method for salt-containing wastewater.
Background
The high-salinity wastewater refers to wastewater with the total salt mass fraction of at least 1%, which is mainly from chemical plants, petroleum and natural gas collection and processing sites and the like, and contains various substances (including salt, oil, organic heavy metals and radioactive substances). The production route of the salt-containing wastewater is wide, the water quantity is increased year by year, and the removal of organic pollutants in the salt-containing wastewater is of great importance to environmental management.
However, the existing salt-containing wastewater evaporative crystallization device cannot effectively remove impurities in the salt-containing wastewater, and has high energy consumption and greatly increased cost.
Therefore, the problem to be solved by the technical personnel in the field is to provide a double-stage MVR single-effect forced circulation evaporation production device and method for salt-containing wastewater with low energy consumption.
Disclosure of Invention
In view of this, the invention provides a double-stage MVR single-effect forced circulation evaporation production device and method for salt-containing wastewater, which can reduce energy consumption and improve treatment effect.
In order to achieve the purpose, the invention adopts the following technical scheme:
a double-stage MVR single-effect forced circulation evaporation production device for salt-containing wastewater comprises a raw material tank, a feeding pump, a two-stage preheater, a first-stage heating chamber, a first-stage separation chamber, a first-stage circulating pump, a second-stage heating chamber, a second-stage separation chamber, a second-stage circulating pump, a third-stage heating chamber, a discharging pump, a thickener, a centrifuge and a mother liquor pool which are sequentially connected through pipelines; the saturated raw steam storage tank is respectively connected with the two-stage preheater, the first-stage heating chamber, the second-stage heating chamber and the third-stage heating chamber through pipelines; the vacuum pump is respectively connected with the primary heating chamber and the secondary heating chamber through pipelines; the first-stage circulating pump is connected with the top of the first-stage heating chamber through a pipeline; the second-stage circulating pump is connected with the top of the second-stage heating chamber through a pipeline; and a mother liquid pump is installed in the mother liquid pool and is connected with the raw material tank through a pipeline.
The primary heating chamber, the condensed water tank and the condensed water pump are connected in sequence through pipelines; the two-stage preheater is connected with the condensed water tank through a pipeline; and the condensate pump is connected with the third-stage heating chamber through a pipeline.
The device further comprises a compressor, wherein the compressor is respectively connected with the first-stage heating chamber, the first-stage separation chamber, the second-stage heating chamber and the second-stage separation chamber through pipelines.
And furthermore, the device also comprises a third-stage separation chamber and a third-stage axial flow pump, wherein the third-stage separation chamber and the third-stage axial flow pump are connected with the third-stage heating chamber through pipelines.
Furthermore, the number of the thickeners, the centrifuges and the mother liquor pool is two, and each thickener is communicated with one mother liquor pool through one centrifuge; the volume of each mother liquor pool is 5-15m3。
Further, the volume of the first-stage heating chamber is 3000-3500m3The diameter of the primary separation chamber is 3500-4500 mm; the volume of the secondary heating chamber is 2500-3The diameter of the secondary separation chamber is 3500-4500 mm; the volume of the three-stage heating chamber is 300-500m3The diameter of the three-stage separation chamber is 3000-4000 mm; the volume of the raw steam preheater of the two-stage preheater is 70-90m3(ii) a The volume of the condensed water tank is 9-12m3。
Further, the power of the compressor is 3000-35000kw, and the material quality is 316L; the flow rate of the primary circulating pump is 720-780m3H, the lift is 20-30m, the power is 120-; the flow rate of the secondary circulating pump is 740-760m3H, the lift is 20-30m, the power is 120-; the flow rate of the three-stage axial flow pump is 3500-4500m3H, the lift is 3.5-4.5m, the power is 120-140kw, and the material is 316L; the flow rate of the feeding pump is 110-135m3H, the lift is 20-38m, the power is 20-30kw, and the material quality is 316L; the flow rate of the discharge pump is 10-20m3The lift is 26-40m, the power is 4-7kw, and the material is 316L; the flow rate of the condensed water pump is 100-140m3H, the lift is 25-35m, the power is 15-22kw, and the material quality is 316L; the pumping capacity of the vacuum pump is 400-600m3The power is 10-20kw, and the material is carbon steel; the volume of the thickener is 4-6m3The power is 4-6kw, and the material quality is 316L; the power of the centrifugal machine is 10-15kw, and the material quality is 316L.
The method performed according to the double-stage MVR single-effect forced circulation evaporation production device for the salt-containing wastewater comprises the following steps:
s1, conveying the salt-containing wastewater into a raw material tank, firstly conveying the salt-containing wastewater into a two-stage preheater through a feeding pump, preheating the salt-containing wastewater to a boiling point, then evaporating the salt-containing wastewater in a tube pass of a first-stage heating chamber, and introducing saturated raw steam in a saturated raw steam storage tank into shell passes of the first-stage heating chamber, a second-stage heating chamber and a third-stage heating chamber to heat the material liquid;
s2, circularly concentrating the materials in the first-stage heating chamber to a certain concentration, then feeding the materials into the second-stage heating chamber for re-evaporation, feeding the materials into the third-stage heating chamber after the materials are concentrated to a certain concentration, finally pumping the materials into a thickener by a discharge pump after the materials are concentrated to a specified concentration, then feeding the materials into a centrifugal machine for centrifugal separation to obtain a solid product, and returning the mother liquor to the raw material tank;
s3, the secondary steam generated after the solution in the primary heating chamber is heated and evaporated and enters the primary separation chamber enters a compressor, meanwhile, the secondary steam generated after the solution in the secondary heating chamber is heated and evaporated and enters the secondary separation chamber enters the compressor, the solution in the tube pass of the tertiary heating chamber is heated and evaporated, and the generated secondary steam is used as a heat source of other methods and equipment;
and S4, exchanging heat between the condensate water of the shell pass of the first-stage heating chamber, the second-stage heating chamber and the third-stage heating chamber and the raw material through the two-stage preheater, and then entering a condensate water tank through a steam trap for recycling.
Further, the primary evaporation operation has the heating steam pressure of 0.08-0.09Mpa, the heating steam temperature of 80-120 ℃, the raw material temperature of 801-90 ℃, the secondary steam pressure of 0.05-0.06Mpa, the secondary steam temperature of 70-90 ℃, the liquid phase temperature of 70-90 ℃, the effective temperature difference of 10-20 ℃ and the water evaporation amount of 43000 and 47000 kg/h; the secondary evaporation operation comprises the steps of heating the raw material at the temperature of between 70 and 90 ℃ under the steam pressure of between 0.08 and 0.09MPa, heating the raw material at the temperature of between 90 and 130 ℃ under the secondary steam pressure of between 0.05 and 0.06MPa, heating the secondary steam at the temperature of between 70 and 95 ℃ under the liquid phase temperature of between 80 and 103 ℃, controlling the effective temperature difference of between 10 and 15 ℃ and controlling the amount of water to be 43000 and 47000 kg/h; the three-stage evaporation operation has the heating steam pressure of 0.5-0.6 Mpa, the heating steam temperature of 135-.
Therefore, compared with the prior art, the invention provides a double-stage MVR single-effect forced circulation evaporation production device and method for salt-containing wastewater, and the invention comprises the following steps:
1) the comprehensive energy consumption is lower: an MVR mechanical recompression evaporation crystallization system is adopted, saturated steam is introduced into an evaporation crystallizer at one time, secondary steam after feed liquid is boiled is compressed by adopting an MVR technology for recycling, the saturated steam is not used any more, and energy consumption can be greatly saved;
2) the evaporation effect is better: due to the adoption of three-stage evaporation, impurities in the salt-containing wastewater can be completely removed, and clean water capable of being reused is obtained.
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, it is obvious that the drawings in the following description are only embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the provided drawings without creative efforts.
FIG. 1 is a schematic process flow diagram of a double-stage MVR single-effect forced circulation evaporation production device for salt-containing wastewater provided by the 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 obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.
As shown in fig. 1, the embodiment of the invention discloses a two-stage MVR single-effect forced circulation evaporation production device for salt-containing wastewater, which comprises a raw material tank 1, a feeding pump 2, a two-stage preheater 3, a one-stage heating chamber 4, a one-stage separation chamber 5, a one-stage circulating pump 6, a two-stage heating chamber 7, a two-stage separation chamber 8, a two-stage circulating pump 9, a three-stage heating chamber 10, a discharging pump 11, a thickener 12, a centrifuge 13 and a mother liquor pool 14 which are connected in sequence through pipelines; the saturated raw steam storage tank 15 is respectively connected with the two-stage preheater 3, the first-stage heating chamber 4, the second-stage heating chamber 7 and the third-stage heating chamber 10 through pipelines; the vacuum pump 16 is respectively connected with the first-stage heating chamber 4 and the second-stage heating chamber 7 through pipelines; the first-stage circulating pump 6 is connected with the top of the first-stage heating chamber 4 through a pipeline; the second-stage circulating pump 9 is connected with the top of the second-stage heating chamber 7 through a pipeline; a mother liquor pump 17 is installed in the mother liquor pool 14, and the mother liquor pump 17 is connected with the raw material tank 1 through a pipeline.
Specifically, the heating device also comprises a condensed water tank 18 and a condensed water pump 19, wherein the primary heating chamber 4, the condensed water tank 18 and the condensed water pump 19 are sequentially connected through pipelines; the two-stage preheater 3 is connected with the condensed water tank 18 through a pipeline; the condensate pump 19 is connected with the third-stage heating chamber 10 through a pipeline, and the condensate pump 19 is used for discharging waste condensate.
Specifically, the device further comprises a compressor 20, and the compressor 20 is respectively connected with the first-stage heating chamber 4, the first-stage separation chamber 5, the second-stage heating chamber 7 and the second-stage separation chamber 8 through pipelines.
Specifically, the device further comprises a third-stage separation chamber 21 and a third-stage axial flow pump 22, wherein the third-stage separation chamber 21 and the third-stage axial flow pump 22 are connected with the third-stage heating chamber 10 through pipelines.
Specifically, the number of the thickeners 12, the centrifuges 13 and the mother liquor pools 14 is two, and each thickener 12 is communicated with one mother liquor pool 14 through one centrifuge 13; the volume of each mother liquor pool 14 is 5-15m3。
Specifically, the volume of the first-stage heating chamber 4 is 3000-3500m3The diameter of the first-stage separation chamber 5 is 3500-4500 mm; the volume of the secondary heating chamber 7 is 2500-3500m3The diameter of the secondary separation chamber 8 is 3500-4500 mm; the volume of the three-stage heating chamber 10 is 300-500m3The diameter of the third-stage separation chamber 21 is 3000-4000 mm; the volume of the raw steam preheater of the two-stage preheater 3 is 70-90m3(ii) a The volume of the condensed water tank 18 is 9-12m3。
In this embodiment, the primary heating chamber 4 has a volume of 3000m3(ii) a The diameter of the primary separation chamber 5 is 4000 mm; the volume of the secondary heating chamber 7 is 3000m3(ii) a The diameter of the secondary separation chamber 8 is 4000 mm; the volume of the three-stage heating chamber 10 is 400m3(ii) a The diameter of the third-stage separation chamber 21 is 3500 mm; raw steam preheater volume 80m3(ii) a Condensed water tank 18 m in volume3。
Specifically, the power of the compressor 20 is 3000-35000kw, and the material quality is 316L; the flow rate of the primary circulating pump 6 is 720-780m3H, the lift is 20-30m, the power is 120-; the flow rate of the two-stage circulating pump 9 is 740 and 760m3H, the lift is 20-30m, the power is 120-; the flow rate of the three-stage axial flow pump 22 is 3500-4500m3H, the lift is 3.5-4.5m, the power is 120-140kw, and the material is 316L; the flow rate of the feeding pump 2 is 110-135m3H, the lift is 20-38m, the power is 20-30kw, and the material quality is 316L; the flow of the discharging pump 11 is 10-20m3The lift is 26-40m, the power is 4-7kw, and the material is 316L; the flow rate of the condensate pump 19 is 100-140m3H, the lift is 25-35m, the power is 15-22kw, and the material quality is 316L; the pumping capacity of the vacuum pump 16 is 400-600m3The power is 10-20kw, and the material is carbon steel; the volume of the thickener 12 is 4-6m3The power is 4-6kw, the material is 316L; the centrifuge 13 has power of 10-15kw and material quality of 316L.
In the present embodiment, the compressor 20 has a power of 3200 kw; the flow rate of the first-stage circulating pump 6 is 742m3H, head 25m, power 132 kw; the flow rate of the second-stage circulating pump 9 is 742m3H, lift 25m, power 132 kw; the flow rate of the three-stage axial flow pump 22 is 4000m3H, head 4m, power 132 kw; the flow rate of the feeding pump 2 is 120m3H, lift 24m, power 22 kw; the flow of the discharging pump 11 is 15m3H, lift 32m and power 5.5 kw; the flow of the condensate pump 19 is 120m3H, head 32m, power 18.5 kw; the air pumping capacity of the vacuum pump 16 is 500m3/h, and the power is 15 kw; the volume of the thickener is 12m3The power is 5.5 kw; the power of the centrifugal machine 13 is 11 kw; all pipelines and valves were made of 316L.
The working process is as follows: raw materials from a tower kettle are conveyed into a raw material tank 1, conveyed into a two-stage preheater 3 through a feeding pump 2 and then enter a condensed water tank 18, and then sequentially conveyed into a first-stage heating chamber 4, a first-stage separation chamber 5, a first-stage circulating pump 6, a second-stage heating chamber 7, a second-stage separation chamber 8, a second-stage circulating pump 9, a third-stage heating chamber 10, a third-stage separation chamber 21 and a third-stage axial flow pump 22, secondary steam obtained from the top of the third-stage separation chamber 21 goes to other equipment to be used as a heating medium, other materials are conveyed into two thickeners 12 through a discharging pump 11 and then are respectively conveyed into two centrifuges 13, the obtained product enters a mother liquid tank 14, mother liquid in the mother liquid tank 14 can be conveyed back into the raw material tank 1 through a mother liquid pump 17 to be recycled, saturated raw steam is used as the heating medium of the first-stage heating chamber 4 (a first-stage heater), the second-stage heater 7 (a second-stage heater) and the third-stage heating chamber 10 (a third-stage heater) after passing through the two-stage preheater 3, the materials obtained from the tops of the first-stage separation chamber 5 and the second-stage separation chamber 8 are pumped back to the first-stage heating chamber 4 and the second-stage heating chamber 7 by the compressor 20 for recycling.
The embodiment of the invention also discloses a method for utilizing the double-stage MVR single-effect forced circulation evaporation production device for the salt-containing wastewater, which comprises the following steps:
s1, conveying the salt-containing wastewater into a raw material tank 1, firstly conveying the salt-containing wastewater to a two-stage preheater 3 through a feeding pump 2, wherein the two-stage preheater 3 comprises a condensate water preheater and a raw steam preheater, preheating the salt-containing wastewater to a boiling point, then evaporating the salt-containing wastewater in a tube side of a first-stage heating chamber 4, and simultaneously introducing saturated raw steam in a saturated raw steam storage tank 15 into shell sides of the first-stage heating chamber 4, a second-stage heating chamber 7 and a third-stage heating chamber 10 to heat the feed liquid;
in the step, the first-stage evaporation operation is carried out under the conditions that the heating steam pressure is 0.08-0.09Mpa, the heating steam temperature is 80-120 ℃ and the raw material temperature is 801-90 ℃.
In this example, the primary evaporation operation heated the steam pressure to 0.0845Mpa, the steam temperature to 100 ℃, the heat of vaporization to 2269.7kJ per kg, and the feed temperature to 85 ℃.
S2, circularly concentrating the materials in the first-stage heating chamber 4 to a certain concentration, then feeding the materials into the second-stage heating chamber 7 for re-evaporation, feeding the materials into the third-stage heating chamber 10 after the materials are concentrated to a certain concentration, finally pumping the materials into the thickener 12 by the discharge pump 11 after the materials are concentrated to a specified concentration, then feeding the materials into the centrifuge 13 for centrifugal separation to obtain a solid product, and returning the mother liquor to the raw material tank 1; due to the adoption of the three-stage evaporation system, impurities in the salt-containing wastewater can be completely removed, and clean water which can be reused is obtained;
in the step, the pressure of heating steam in the second-stage evaporation operation is 0.08-0.09Mpa, the temperature of the heating steam is 90-130 ℃, and the temperature of the raw material is 70-90 ℃; the three-stage evaporation operation has the heating steam pressure of 0.5-0.6 Mpa, the heating steam temperature of 135-175 ℃ and the raw material temperature of 75-95 ℃.
In the present example, the secondary evaporation operation was carried out at a heating steam pressure of 0.0845Mpa, a heating steam temperature of 100 ℃, a heating steam heat of vaporization of 2269.7 kJ/kg, and a feedstock temperature of 85 ℃; the three-stage evaporation operation is carried out, the heating steam pressure is 0.5 Mpa, the heating steam temperature is 151 ℃, the heating steam vaporization heat is 2133.6 kJ/kg, and the raw material temperature is 86 ℃.
S3, the secondary steam generated after the solution in the first-stage heating chamber 4 is heated and evaporated and enters the first-stage separation chamber 5 enters the compressor 20, meanwhile, the secondary steam generated after the solution in the second-stage heating chamber 7 is heated and evaporated and enters the second-stage separation chamber 8 enters the compressor 20, the solution in the tube pass of the third-stage heating chamber 10 is heated and evaporated, and the generated secondary steam is used as a heat source of other method equipment (a front-stage process tower reboiler);
in the step, the pressure of secondary steam in the primary evaporation operation is 0.05-0.06Mpa, the temperature of the secondary steam is 70-90 ℃, the temperature of a liquid phase is 70-90 ℃, the effective temperature difference is 10-20 ℃, and the amount of water evaporated is 43000 and 47000 kilograms per hour; the secondary steam pressure of the secondary evaporation operation is 0.05-0.06Mpa, the secondary steam temperature is 70-95 ℃, the liquid phase temperature is 80-103 ℃, the effective temperature difference is 10-15 ℃, and the water evaporation amount is 43000 and 47000 kilograms per hour; the secondary steam pressure of the three-stage evaporation operation is 0.09-0.17Mpa, the secondary steam temperature is 85-110 ℃, the liquid phase temperature is 100-120 ℃, the effective temperature difference is 30-45 ℃, and the water evaporation amount is 12000 kg/h.
In the embodiment, the secondary steam pressure of the primary evaporation operation is 0.0556Mpa, the secondary steam temperature is 84 ℃, the secondary steam vaporization heat is 2298kJ per kg, the secondary steam specific volume is 2.9348m, 3 per kg, the liquid phase temperature is 85 ℃, the effective temperature difference is 15 ℃, and the water evaporation amount is 45000 kg/h; the secondary steam pressure of the secondary evaporation operation is 0.0556Mpa (absolute), the secondary steam temperature is 84 ℃, the secondary steam vaporization heat is 2298 kJ/kg, the secondary steam specific volume is 2.9348m 3/kg, the liquid phase temperature is 86 ℃, the effective temperature difference is 13 ℃, and the water vaporization quantity is 43000 kg/h; the secondary steam pressure of the three-stage evaporation operation is 0.1MPa (absolute), the secondary steam temperature is 100 ℃, the secondary steam vaporization heat is 2108.2 kJ/kg, the secondary steam specific volume is 1.67m 3/kg, the liquid phase temperature is 112 ℃, the effective temperature difference is 37 ℃, and the water vaporization quantity is 10000 kg/h.
S4, the shell pass condensed water of the first-stage heating chamber 4, the second-stage heating chamber 7 and the third-stage heating chamber 10 exchanges heat with the raw material through the two-stage preheater 3, and then enters the condensed water tank 19 through the steam trap for recycling.
The embodiments in the present description are described in a progressive manner, each embodiment focuses on differences from other embodiments, and the same and similar parts among the embodiments are referred to each other. The device disclosed by the embodiment corresponds to the method disclosed by the embodiment, so that the description is simple, and the relevant points can be referred to the method part for description.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (9)
1. A two-stage MVR single-effect forced circulation evaporation production device for salt-containing wastewater is characterized by comprising a raw material tank, a feeding pump, a two-stage preheater, a one-stage heating chamber, a one-stage separation chamber, a one-stage circulating pump, a two-stage heating chamber, a two-stage separation chamber, a two-stage circulating pump, a three-stage heating chamber, a discharging pump, a thickener, a centrifuge and a mother liquor pool which are sequentially connected through pipelines; the saturated raw steam storage tank is respectively connected with the two-stage preheater, the first-stage heating chamber, the second-stage heating chamber and the third-stage heating chamber through pipelines; the vacuum pump is respectively connected with the primary heating chamber and the secondary heating chamber through pipelines; the first-stage circulating pump is connected with the top of the first-stage heating chamber through a pipeline; the second-stage circulating pump is connected with the top of the second-stage heating chamber through a pipeline; and a mother liquid pump is arranged in the mother liquid pool, and the mother liquid pump is connected with the raw material tank through a pipeline.
2. The two-stage MVR single-effect forced circulation evaporation production device for saline wastewater according to claim 1, further comprising a condensed water tank and a condensed water pump, wherein the first-stage heating chamber, the condensed water tank and the condensed water pump are sequentially connected through a pipeline; the two-stage preheater is connected with the condensed water tank through a pipeline; the condensate pump is connected with the third-stage heating chamber through a pipeline.
3. The apparatus for two-stage MVR single-effect forced circulation evaporation production of saline wastewater according to claim 2, further comprising a compressor, wherein the compressor is respectively connected with the first-stage heating chamber, the first-stage separation chamber, the second-stage heating chamber and the second-stage separation chamber through pipes.
4. The double-stage MVR single-effect forced circulation evaporation production device of saline wastewater according to claim 3, further comprising a third stage separation chamber and a third stage axial flow pump, wherein the third stage separation chamber and the third stage axial flow pump are both connected with the third stage heating chamber through a pipeline.
5. The double-stage MVR single-effect forced circulation evaporation production device for the saline wastewater according to claim 1, wherein the number of the thickeners, the centrifuges and the mother liquor pool is two, and each thickener is connected and communicated with one mother liquor pool through one centrifuge; the volume of each mother liquor pool is 5-15m3。
6. The dual stage MVR single effect forced circulation evaporation of saline wastewater according to claim 4The production device is characterized in that the volume of the primary heating chamber is 3000-3500m3The diameter of the primary separation chamber is 3500-4500 mm; the volume of the secondary heating chamber is 2500-3500m3The diameter of the secondary separation chamber is 3500-4500 mm; the volume of the three-stage heating chamber is 300-500m3The diameter of the three-stage separation chamber is 3000-4000 mm; the volume of the raw steam preheater of the two-stage preheater is 70-90m3(ii) a The volume of the condensed water tank is 9-12m3。
7. The two-stage MVR single-effect forced circulation evaporation production device of saline wastewater as claimed in claim 4, wherein the compressor power is 3000-35000kw, the material is 316L; the flow rate of the primary circulating pump is 720-780m3H, the lift is 20-30m, the power is 120-; the flow rate of the secondary circulating pump is 740-760m3H, the lift is 20-30m, the power is 120-; the flow rate of the three-stage axial flow pump is 3500-4500m3H, the lift is 3.5-4.5m, the power is 120-140kw, and the material is 316L; the flow rate of the feeding pump is 110-3The lift is 20-38m, the power is 20-30kw, and the material is 316L; the flow of the discharge pump is 10-20m3H, the lift is 26-40m, the power is 4-7kw, and the material quality is 316L; the flow rate of the condensed water pump is 100-140m3The lift is 25-35m, the power is 15-22kw, and the material is 316L; the pumping rate of the vacuum pump is 400-600m3The power is 10-20kw, and the material is carbon steel; the volume of the thickener is 4-6m3The power is 4-6kw, and the material quality is 316L; the power of the centrifugal machine is 10-15kw, and the material quality is 316L.
8. The method for the double-stage MVR single-effect forced circulation evaporation production unit of salt-containing wastewater according to any one of claims 1 to 7, which comprises the following steps:
s1, conveying the salt-containing wastewater into a raw material tank, firstly conveying the salt-containing wastewater to a two-stage preheater through a feeding pump, preheating the salt-containing wastewater to a boiling point, then introducing the salt-containing wastewater into a tube side of a first-stage heating chamber for evaporation, and simultaneously introducing saturated raw steam in a saturated raw steam storage tank into shell sides of the first-stage heating chamber, a second-stage heating chamber and a third-stage heating chamber to heat the material liquid;
s2, circularly concentrating the materials in the first-stage heating chamber to a certain concentration, then feeding the materials into the second-stage heating chamber for re-evaporation, feeding the materials into the third-stage heating chamber after the materials are concentrated to a certain concentration, finally pumping the materials into a thickener by a discharge pump after the materials are concentrated to a specified concentration, then feeding the materials into a centrifuge for centrifugal separation to obtain a solid product, and returning the mother liquor to the raw material tank;
s3, the secondary steam generated after the solution in the primary heating chamber is heated and evaporated and enters the primary separation chamber enters a compressor, meanwhile, the secondary steam generated after the solution in the secondary heating chamber is heated and evaporated and enters the secondary separation chamber enters the compressor, the solution in the tube pass of the tertiary heating chamber is heated and evaporated, and the generated secondary steam is used as a heat source of other methods and equipment;
and S4, exchanging heat between the condensate water of the shell pass of the first-stage heating chamber, the second-stage heating chamber and the third-stage heating chamber and the raw material through the two-stage preheater, and then entering a condensate water tank through a steam trap for recycling.
9. The method as claimed in claim 8, wherein the primary evaporation operation is carried out under a heating steam pressure of 0.08 to 0.09Mpa, a heating steam temperature of 80 to 120 ℃, a feedstock temperature of 801 to 90 ℃, a secondary steam pressure of 0.05 to 0.06Mpa, a secondary steam temperature of 70 to 90 ℃, a liquid phase temperature of 70 to 90 ℃, an effective temperature difference of 10 to 20 ℃, and an evaporation water amount of 43000 and 47000 kg/h; the pressure of heating steam in the secondary evaporation operation is 0.08-0.09Mpa, the temperature of the heating steam is 90-130 ℃, the temperature of the raw material is 70-90 ℃, the pressure of secondary steam is 0.05-0.06Mpa, the temperature of the secondary steam is 70-95 ℃, the temperature of a liquid phase is 80-103 ℃, the effective temperature difference is 10-15 ℃, and the amount of the water is 43000 and 47000 kg/h; the three-stage evaporation operation has the heating steam pressure of 0.5-0.6 Mpa, the heating steam temperature of 135-.
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