CN216986314U - Evaporation concentration system - Google Patents
Evaporation concentration system Download PDFInfo
- Publication number
- CN216986314U CN216986314U CN202220033188.XU CN202220033188U CN216986314U CN 216986314 U CN216986314 U CN 216986314U CN 202220033188 U CN202220033188 U CN 202220033188U CN 216986314 U CN216986314 U CN 216986314U
- Authority
- CN
- China
- Prior art keywords
- subsystem
- outlet
- inlet
- pump
- evaporator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000001704 evaporation Methods 0.000 title claims abstract description 91
- 230000008020 evaporation Effects 0.000 title claims abstract description 90
- 239000007788 liquid Substances 0.000 claims abstract description 53
- 230000006835 compression Effects 0.000 claims abstract description 38
- 238000007906 compression Methods 0.000 claims abstract description 38
- 239000002994 raw material Substances 0.000 claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 34
- 239000000463 material Substances 0.000 claims description 12
- 238000007599 discharging Methods 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 4
- 239000007789 gas Substances 0.000 abstract description 17
- 239000002918 waste heat Substances 0.000 abstract description 17
- 238000005265 energy consumption Methods 0.000 abstract description 9
- 238000011084 recovery Methods 0.000 abstract description 4
- 239000002173 cutting fluid Substances 0.000 abstract description 3
- 239000010842 industrial wastewater Substances 0.000 abstract description 3
- 238000003754 machining Methods 0.000 abstract description 3
- 230000002285 radioactive effect Effects 0.000 abstract description 3
- 239000013535 sea water Substances 0.000 abstract description 3
- 239000002351 wastewater Substances 0.000 abstract description 3
- 239000000243 solution Substances 0.000 description 24
- 230000005494 condensation Effects 0.000 description 10
- 238000009833 condensation Methods 0.000 description 10
- 230000009471 action Effects 0.000 description 8
- 239000013589 supplement Substances 0.000 description 7
- 238000000034 method Methods 0.000 description 6
- 238000001514 detection method Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 230000008859 change Effects 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000010963 304 stainless steel Substances 0.000 description 1
- 229910000589 SAE 304 stainless steel Inorganic materials 0.000 description 1
- 230000002159 abnormal effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000012527 feed solution Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 238000005461 lubrication Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
Images
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to the technical field of evaporation concentration, and provides an evaporation concentration system, which comprises: the preheating subsystem is used for preheating the raw material liquid; the evaporation concentration subsystem is used for carrying out evaporation concentration on the preheated raw material liquid; and the compression enthalpy-increasing subsystem is used for compressing enthalpy-increasing gas exhausted by the evaporation concentration subsystem, and the gas subjected to compression enthalpy-increasing enters the evaporation concentration subsystem for heat exchange. The evaporation concentration subsystem provided by the utility model is suitable for the fields of machining cutting fluid waste water concentration, radioactive seawater concentration, industrial waste water concentration and the like. According to the evaporation concentration subsystem provided by the utility model, the compression enthalpy-increasing subsystem is arranged, and the waste heat of the secondary steam generated by the evaporation concentration subsystem is recycled, so that the energy consumption of the evaporation concentration subsystem is greatly saved, and the utilization efficiency of the waste heat recovery is improved.
Description
Technical Field
The utility model relates to the technical field of evaporation concentration, in particular to an evaporation concentration system.
Background
The principle of the mechanical vapor recompression technology is that low-grade steam passes through a compressor, so that the temperature and the pressure of the low-grade steam are improved, the enthalpy value of the low-grade steam is increased, the low-grade steam enters a heat exchanger to exchange heat with raw material liquid, the heated raw material liquid is evaporated by utilizing the latent heat of the steam to generate low-grade steam, the low-grade steam enters the compressor to be compressed into high-grade steam, and continuous evaporation concentration is realized, so that the energy conservation of a system is realized.
In the existing industry, the full-automatic evaporation concentration device based on electric drive has high energy consumption, the utilization of waste heat, particularly the waste heat of secondary steam, is insufficient, the heat compensation adopts an electric boiler or steam for heat compensation, the system depends on external energy conditions seriously, manual or semi-automatic operation is mostly adopted in the system, and the requirement on manpower is high.
SUMMERY OF THE UTILITY MODEL
The utility model provides an evaporation concentration system, which is used for solving the defects of high energy consumption and insufficient utilization of waste heat of secondary steam of the evaporation concentration system in the prior art.
The present invention provides an evaporative concentration system comprising: the preheating subsystem is used for preheating the raw material liquid; the evaporation concentration subsystem is used for carrying out evaporation concentration on the preheated raw material liquid; and the compression enthalpy-increasing subsystem is used for compressing enthalpy-increasing gas exhausted by the evaporation concentration subsystem, and the gas subjected to compression enthalpy-increasing enters the evaporation concentration subsystem for heat exchange.
According to the present invention, there is provided an evaporative concentration system, the preheating sub-system comprising: the system comprises a material tank, a first pump, a first preheater and a second preheater; the outlet of the material tank is connected with the inlet of the first pump, the outlet of the first pump is connected with the first inlet of the first preheater, the first outlet of the first preheater is connected with the first inlet of the second preheater, and the first outlet of the second preheater is connected with the inlet of the evaporation concentration subsystem.
According to the evaporation concentration system provided by the utility model, the evaporation concentration subsystem comprises an evaporator, a first inlet of the evaporator is connected with a first outlet of the second preheater, a first outlet of the evaporator is connected with an inlet of the compression enthalpy-increasing subsystem, a second inlet of the evaporator is connected with an outlet of the compression enthalpy-increasing subsystem, a second outlet of the evaporator is connected with a second inlet of the first preheater, and a second outlet of the first preheater is used for discharging non-condensable gas.
According to the evaporation concentration system provided by the utility model, the evaporation concentration subsystem further comprises an exhaust valve, an inlet of the exhaust valve is connected with the second outlet of the evaporator, and an outlet of the exhaust valve is connected with the second inlet of the first preheater.
According to the present invention, there is provided an evaporation concentration system, wherein the compression enthalpy-increasing subsystem comprises: the inlet of the gas-liquid separator is connected with the first outlet of the evaporator, the outlet of the gas-liquid separator is connected with the first inlet of the compressor, and the outlet of the compressor is connected with the second inlet of the evaporator.
According to the evaporation concentration system provided by the utility model, the compression enthalpy-increasing subsystem further comprises a one-way valve, an inlet of the one-way valve is connected with an outlet of the compressor, and an outlet of the one-way valve is connected with a second inlet of the evaporator.
According to the present invention, there is provided an evaporation concentration system, further comprising: a condensing tank, an electric heater and a second pump; the compression enthalpy-adding subsystem further comprises a third pump; the third export of evaporimeter with the access connection of condensate tank, the first export of condensate tank with the third access connection of evaporimeter, the second export of condensate tank with the access connection of third pump, the export of third pump with the second access connection of compressor, the third export of condensate tank with the access connection of second pump, the export of second pump with the second access connection of second preheater, wherein, the second export of second preheater is used for discharging the comdenstion water, the electric heater sets up in the condensate tank.
According to the present invention, there is provided an evaporation concentration system, the evaporation concentration subsystem further comprising: the evaporator comprises a concentrated solution tank and a fourth pump, wherein an inlet of the concentrated solution tank is connected with a fourth outlet of the evaporator, an outlet of the concentrated solution tank is connected with an inlet of the fourth pump, a first outlet of the fourth pump is used for discharging concentrated solution, and a second outlet of the fourth pump is connected with a fourth inlet of the evaporator.
According to the evaporation concentration system provided by the utility model, the evaporation concentration system further comprises a controller, and the controller is in communication connection with the preheating subsystem, the evaporation concentration subsystem and the compression enthalpy-increasing subsystem.
According to the evaporation concentration system provided by the utility model, the plurality of pipelines of the compressor are respectively provided with the switch valve and the flowmeter, the flowmeter sends a signal to the controller, and the controller controls the switch valve to be opened according to the signal.
The evaporation concentration subsystem provided by the utility model is suitable for the fields of machining cutting fluid waste water concentration, radioactive seawater concentration, industrial waste water concentration and the like. According to the evaporation concentration subsystem provided by the utility model, the compression enthalpy-increasing subsystem is arranged, and the waste heat of the secondary steam generated by the evaporation concentration subsystem is recycled, so that the energy consumption of the evaporation concentration subsystem is greatly saved, and the utilization efficiency of the waste heat recovery is improved.
Drawings
In order to more clearly illustrate the technical solutions of the present invention or the prior art, the drawings needed for the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and those skilled in the art can also obtain other drawings according to the drawings without creative efforts.
FIG. 1 is a schematic diagram of an evaporative concentration system provided by the present invention;
FIG. 2 is a schematic view of the evaporator shown in FIG. 1;
reference numerals are as follows:
10: a preheating subsystem; 11: a material tank; 12: a first pump; 13: a first preheater; 14: a second preheater; 20: an evaporation concentration subsystem; 21: an evaporator; 22: a condensing tank; 23: a second pump; 24: a concentrated solution tank; 25: a fourth pump; 26: an electric heater; 27: an exhaust valve; 30: a compression enthalpy-increasing subsystem; 31: a gas-liquid separator; 32: a compressor; 33: a one-way valve; 34: a third pump; 211: an inner circulation pipe; 212: a heat exchange tube.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention clearer, the technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings, and it is obvious that the described embodiments are some, but not all embodiments of the present invention. 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.
The features of the terms first and second in the description and in the claims of the utility model may explicitly or implicitly include one or more of these features. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
The evaporative concentration system of the present invention is described below with reference to fig. 1 and 2.
As shown in fig. 1, in one embodiment of the present invention, an evaporative concentration system includes: a preheating subsystem 10, an evaporation concentration subsystem 20 and a compression enthalpy-increasing subsystem 30. The preheating subsystem 10 is used for preheating the raw material liquid, the evaporation concentration subsystem 20 is used for evaporating and concentrating the preheated raw material liquid, the compression enthalpy-increasing subsystem 30 is used for compressing and increasing enthalpy of gas exhausted by the evaporation concentration subsystem 20, and the gas after compression and increasing enthalpy enters the evaporation concentration subsystem 20 for heat exchange.
Specifically, the raw material liquid is preheated in the preheating subsystem 10 and then enters the evaporation concentration subsystem 20, the raw material liquid is heated in the evaporation concentration subsystem 20 and then evaporated, the vapor generated by evaporation enters the compression enthalpy-increasing subsystem 30 to compress enthalpy so as to increase the temperature and pressure of the vapor, the formed high-grade vapor enters the evaporation concentration subsystem 20 to serve as a heat source for heat exchange, the vapor after heat exchange undergoes phase change to release latent heat to form condensed water, a part of the condensed water enters the preheating subsystem 10 to recover waste heat and then is discharged, a part of the condensed water enters the compression enthalpy-increasing subsystem 30 to lubricate a compressor 32 in the compression enthalpy-increasing subsystem 30, and the part of the condensed water enters the evaporation concentration subsystem 20 after cooling, and discharging the concentrated solution reaching the concentration multiple after evaporation concentration, and performing evaporation concentration again on the concentrated solution not reaching the concentration multiple. In the embodiment, about 90% of the secondary steam generated by the evaporation concentration subsystem is recycled by the compression enthalpy-increasing subsystem, so that the waste heat recycling efficiency is fully improved.
The evaporation concentration subsystem provided by the utility model is suitable for the fields of machining cutting fluid waste water concentration, radioactive seawater concentration, industrial waste water concentration and the like. According to the evaporation concentration subsystem provided by the utility model, the compression enthalpy-increasing subsystem is arranged, and the waste heat of the secondary steam generated by the evaporation concentration subsystem is recycled, so that the energy consumption of the evaporation concentration subsystem is greatly saved, and the utilization efficiency of the waste heat recovery is improved.
As shown in FIG. 1, in one embodiment of the present invention, the preheat subsystem 10 includes: a material tank 11, a first pump 12, a first preheater 13 and a second preheater 14.
Specifically, the raw material liquid enters a first preheater 13 from a material tank 11 under the action of a first pump 12 for primary preheating, then enters a second preheater 14 for secondary preheating until the temperature is 85 ℃, and then enters an evaporation concentration subsystem 20. Further, a second outlet of the first preheater 13 is used for discharging the non-condensable gas, and the first preheater 13 is used for recovering heat carried in the non-condensable gas; the second outlet of the second preheater 14 is used for discharging condensed water, the second preheater 14 is used for recovering heat carried in the condensed water, and the temperature of the raw material liquid is gradually increased after passing through the first preheater 13 and the second preheater 14.
Optionally, the material tank 11 is a vertical storage tank, and the effective volume is 200L and 300L. The first preheater 13 and the second preheater 14 both adopt plate heat exchangers, wherein the heat exchange area of the first preheater 13 is 3m2The heat exchange area of the second preheater 14 is 10m2。
In one embodiment of the present invention, the evaporative concentration subsystem 20 includes an evaporator 21. Specifically, the raw material solution preheated by the second preheater 14 enters the evaporator 21 and is heated to a slightly negative pressure state of about 95 ℃ for evaporation, the vapor generated by evaporation enters the compression enthalpy-increasing subsystem 30 for compression enthalpy-increasing, and the formed high-temperature and high-pressure gas enters the shell side of the evaporator 21 and is used as a heat source of the evaporator 21 for heat exchange. Considering that the feed solution has a boiling temperature rise of 3 ℃, the evaporator 21 has an effective heat exchange temperature difference of 8 ℃ to heat the liquid. After heat exchange in the evaporator 21, the non-condensable gas is discharged after waste heat recovery by the first preheater 13. The steam is subjected to phase change to release latent heat to form condensed water, part of the condensed water is discharged after waste heat is recovered by the preheating subsystem 10, part of the condensed water enters the compression enthalpy-increasing subsystem 30 to lubricate a compressor 32 in the compression enthalpy-increasing subsystem 30, and the part of the condensed water enters the evaporation concentration subsystem 20 after being cooled. And discharging the concentrated solution reaching the concentration multiple after evaporation concentration, and performing evaporation concentration again on the concentrated solution not reaching the concentration multiple.
Further, as shown in fig. 2, the feed liquid in the evaporator 21 adopts an internal circulation mode, an internal circulation pipe 211 with a large diameter is arranged in the evaporator 21, the feed liquid in the heat exchange pipe 212 is driven by steam to rise, and the feed liquid risesThe liquid returns to the lower part of the evaporator 21 through the internal circulation pipe 211 and then enters the heat exchange pipe 212 to be driven by steam to rise, and the process is repeated, so that the liquid is evaporated in an internal circulation mode. Alternatively, in the present embodiment, the heat exchange tube 212 has a size of φ 38x1.5mm and a heat exchange area of 15m2The size of the internal circulation pipe 211 is φ 219x6mm, and the barrel size of the evaporator 21 is φ 916x8 mm.
Further, in an embodiment of the present invention, the evaporation concentration subsystem further comprises a vent valve 27, an inlet of the vent valve 27 is connected with the second outlet of the evaporator 21, and an outlet of the vent valve 27 is connected with the second inlet of the first preheater 13. Optionally, the exhaust valve 27 is an electric type adjusting ball valve, the output and input signals of the valve are 4-20mA, an intelligent actuator is configured, and the driving power supply is 220V.
As shown in fig. 1, in one embodiment of the present invention, the compression enthalpy-addition subsystem 30 includes: a gas-liquid separator 31 and a compressor 32. Specifically, the steam with the temperature of 95 ℃ generated in the evaporator 21 enters the gas-liquid separator 31 for separation, the separated steam enters the compressor 32 for compression and enthalpy increase to improve the temperature and the pressure of the steam, the temperature of the steam at the outlet of the compressor 32 reaches 106 ℃, and the formed high-grade steam enters the shell side of the evaporator 21 and serves as a heat source of the evaporator 21.
Alternatively, the compressor 32 may employ a single screw compressor, a roots compressor, a centrifugal compressor, or the like. In the present embodiment, the compressor 32 is of the single screw type, the motor power is 30kw, and the suction flow rate is 15m3The water spray flow is preferably 1-1.5m3The lubricating oil temperature is preferably from 30 to 80 ℃.
Further, in one embodiment of the present invention, the enthalpy-increasing compression subsystem 30 further includes a check valve 33, an inlet of the check valve 33 is connected to an outlet of the compressor 32, and an outlet of the check valve 33 is connected to an inlet of the evaporator 21. Specifically, the check valve 33 is used to prevent the compressor 32 from being damaged due to vapor backflow caused by an excessive pressure difference between the inlet and the outlet of the compressor 32 when the compressor 32 is in a shutdown state or an abnormal shutdown state and the compressor 32 is in a reverse rotation state.
As shown in FIG. 1, in one embodiment of the present invention, the evaporative concentration subsystem 20 further includes: a condensation tank 22, a second pump 23, and an electric heater 26; the compression enthalpy addition subsystem further includes a third pump 34. Specifically, heat exchange occurs between the steam in the evaporator 21, the steam undergoes phase change to release latent heat, and then forms condensed water, the condensed water enters the condensing tank 22, a part of the condensed water enters the second preheater 14 under the action of the second pump 23 to recover heat in the condensed water, and then the condensed water is discharged from the second outlet of the second preheater 14. Part of the condensed water enters the compressor 32 for lubrication under the action of the third pump 34, and enters the condensing tank 22 after being cooled and cooled.
Further, an electric heater 26 is provided in the condensation tank 22, the electric heater 26 is used for heating the condensed water in the condensation tank 22, and the generated steam enters the evaporator 21 to supplement heat to the evaporator 21. Alternatively, the electric heater 26 is a U-shaped heating electric heating tube, the voltage is 380V, and the power is 24 kW.
Optionally, the condensation tank 22 is a horizontal storage tank with an effective volume of 100-200L.
According to the evaporation concentration system provided by the embodiment of the utility model, the electric heater is arranged in the condensation tank, so that condensed water in the condensation tank can be heated to supplement heat for the evaporator, steam enters the evaporator for heat exchange and then enters the condensation tank again for heating, a circulating system is formed, and the heat supplement efficiency and the heat supplement speed of the evaporation concentration system are improved.
As shown in fig. 1, in one embodiment of the present invention, the evaporative concentration subsystem further comprises: a concentrate tank 24 and a fourth pump 25. After the raw material liquid is evaporated in the evaporator 21, the concentrated liquid reaching the concentration factor enters the concentrated liquid tank 24 and is discharged under the action of the fourth pump 25, and the concentrated liquid not reaching the concentration factor enters the evaporator 21 to continue the evaporation and concentration.
Optionally, the concentrated solution tank 24 adopts a horizontal storage tank, and the effective volume is 100-200L. The first pump 12, the second pump 23 and the fourth pump 25 are single-stage centrifugal pumps, are driven by an electric frequency motor, have the frequency conversion range of 10-50Hz and the flow rate of 0.5m3The power is 1.5 kW.
The operation of the evaporative concentration system provided by the present invention will be described in detail below by taking the embodiment shown in fig. 1 as an example.
Raw material liquid enters a first preheater 13 from a material tank 11 under the action of a first pump 12 for primary preheating, the preheated raw material liquid enters a second preheater 14 for secondary preheating, then the raw material liquid enters an evaporator 21 to be heated and evaporated, steam enters a gas-liquid separator 31 for separation, the separated gas enters a compressor 32 for compression and enthalpy increase, and the gas which becomes high-temperature and high-pressure gas enters a shell pass of the evaporator 21 to be used as a heat source for heat exchange. The concentrated solution after evaporation concentration in the evaporator 21 enters the concentrated solution tank 24, the concentrated solution reaching the concentration multiple is discharged under the action of the fourth pump 25, and the concentrated solution not reaching the concentration multiple enters the evaporator 21 again for evaporation concentration.
The non-condensable gas generated in the evaporation concentration process is discharged after waste heat is recovered by the first preheater 13, condensed water generated in the evaporation concentration process enters the condensing tank 22, part of the condensed water enters the second preheater 14 under the action of the second pump 23, and the condensed water is discharged after the waste heat is recovered by the second preheater 14; part of the condensed water enters the compressor 32 by the third pump 34, lubricates the compressor 32, and finally enters the condensation tank 22. The condensed water in the condensing tank 22 is heated into high-temperature steam under the action of the electric heater 26, the high-temperature steam enters the evaporator 21 to supplement heat for the evaporator 21, the condensed water generated in the evaporation and concentration process enters the condensing tank 22 to form a circulating system to continuously supplement heat for the evaporator 21, the heat exchange capacity of the evaporator 21 is improved, and the energy consumption of an evaporation and concentration system is reduced.
In the embodiment of the utility model, the evaporation concentration system further comprises a controller, the controller adopts the control mode that the first pump 12 is interlocked with the liquid level of the evaporator 21, the second pump 23 is interlocked with the liquid level of the condensing tank 22, the fourth pump 25 is interlocked with the liquid level of the concentrated solution tank 24, the compressor 32 is interlocked with the evaporation flow of the evaporator 21, the electric heater 26 is interlocked with the temperature of the raw material solution of the evaporator 21, and the exhaust valve 27 is interlocked with the gas phase pressure of the evaporator 21, the continuous feeding, discharging and evaporation stable operation of the evaporation concentration system is realized through the interlocking control between each component and the instrument, and the instrument parameters such as temperature, pressure, frequency, flow and the like are converged into the controller, and the stable operation of the process parameters is realized through the controller.
Specifically, liquid level sensors are provided in the evaporator 21, the condensation tank 22, and the concentrate tank 24, the liquid level sensors send signals to a controller, and the controller controls the operating frequencies of the first pump 12, the second pump 23, and the fourth pump 25 to control the liquid levels. Specifically, the first pump 12, the second pump 23 and the fourth pump 25 are driven by variable frequency motors, the liquid level is controlled by adjusting the operating frequency of the pumps, when the liquid level of the evaporator 21 rises, the controller reduces the operating frequency of the first pump 12, otherwise, the operating frequency is increased; when the liquid level of the condensation tank 22 rises, the controller increases the operating frequency of the second pump 23, otherwise, the operating frequency is reduced; the controller increases the operating frequency of the fourth pump 25 when the concentrate tank 24 level increases and decreases it otherwise. The evaporator 21 is provided with a flow meter for detecting the evaporation flow rate, the controller controls the operating frequency of the compressor 32 according to the detection data of the flow meter, when the evaporation flow rate of the evaporator 21 is increased, the controller reduces the operating frequency of the compressor 32, otherwise, the operating frequency is increased. Meanwhile, a temperature sensor is also arranged in the evaporator 21 and used for detecting the temperature in the evaporator 21, the controller controls the power opening degree of the electric heater 26 according to the temperature data, when the temperature of the feed liquid in the evaporator 21 is increased, the controller reduces the power opening degree of the electric heater 26, otherwise, the power opening degree is increased so as to continuously supplement heat for the evaporator 21. The exhaust valve 27 is of a continuously variable type, and when the vapor pressure of the evaporator 21 increases, the controller decreases the valve opening of the exhaust valve 27, and conversely increases the valve opening.
Further, in the embodiment of the present invention, a plurality of pipelines of the compressor 32 are respectively provided with a switch valve and a flow meter, a water spray control chain of the compressor 32 is to prevent the compressor 32 from being damaged due to dirt, a spare pipeline is used for the water spray control chain, a switch valve is respectively arranged at the front and the rear of a filter on each pipeline, when the dirt blockage phenomenon occurs in a pipeline, the flow meter on the pipeline will have flow change, and the controller receives a signal of the flow meter and then controls the other pipeline to be opened.
Optionally, in the embodiment of the utility model, the temperature detection adopts an integrated temperature transmitter, the measuring range is 0-200 ℃, the precision level is 0.25%, and the output signal is 4-20 mA; the pressure detection adopts a small and precise pressure transmitter, the absolute pressure range is 0-400KPA, the precision grade is 0.1 percent, and the output signal is 4-20 mA.
The steam flow detection adopts a precession vortex flowmeter, the measuring range is 0-20m3/min, the precision level is 1.0%, and the output signal is 4-20 mA; the flow detection of feeding, discharging, condensed water and the like adopts a metal rotor flowmeter, the measuring range is 0-500L/H, the precision grade is 1.5%, and the output signal is 4-20 mA.
The liquid level meter adopts a double-flange type liquid level meter, the output signal is 4-20mA, the liquid level measuring range of the evaporator 21 is preferably 0-1000mm, and the liquid level measuring ranges of the condensing tank 22 and the concentrated solution tank 24 are preferably 0-400 mm.
In the above embodiment, all materials contacting the raw material liquid are 316L stainless steel, and the material of the rest of the equipment is 304 stainless steel.
According to the evaporation concentration system provided by the embodiment of the utility model, the compressor is adopted to recycle the waste heat of the secondary steam of the evaporator, so that the energy consumption of the evaporation concentration system is greatly saved, the first preheater and the second preheater are adopted to preheat the raw material liquid, and meanwhile, the waste heat of non-condensable gas and condensed water is recycled, so that the energy consumption is further saved; energy loss in the operation of the evaporator is timely supplemented by the electric heater, the electric heater is arranged in the condensing tank to directly heat and vaporize high-temperature condensed water, the heat supplementing effect is quick, timely and efficient, and meanwhile, the supply of an external water source is saved; the evaporator is internally provided with an internal circulation structure, so that the flow of feed liquid circulation evaporation is reduced, the evaporation is more timely and efficient, the heat loss is lower, the system adopts the design of a full-automatic control system, the energy consumption of pump equipment is further reduced, and a large amount of labor cost is saved.
The evaporation concentration system provided by the embodiment of the utility model has the advantages that all parts are driven by electric power, the efficiency is high, the energy is saved, the material liquid circulation time is short, the evaporation efficiency is high, the structure is compact, the heat is supplemented timely and efficiently, and the system is stable and reliable in operation because the system does not depend on an external water source and a compressor is provided with an anti-reversion one-way valve. Simultaneously, the automatic operation method has the following characteristics that: 1. the system automation has the function of improving the productivity level and the working quality of the enterprise. The control of an automatic system is utilized, the operation is strictly completed according to the preset design requirement, the influence of subjective factors is frequently received when manual operation is avoided, and then the purposes of improving the production quality of products and improving the production efficiency are achieved. 2. The system automation has a precise monitoring and alarming system, and the emergency treatment is more timely and proper, so that some unnecessary loss is avoided. 3. In the aspect of maintenance and debugging, the system automation can well meet the application requirements by adding new field parameters into the control program. 4. The system automation organically links each independent technology and function, so that the function is more complete. 5. The system automation is a knowledge and technology intensive industry, a great deal of heavy labor is realized through machinery, and a great deal of work of people is reduced.
Finally, it should be noted that: the above examples are only intended to illustrate the technical solution of the present invention, and not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (10)
1. An evaporative concentration system, comprising:
the preheating subsystem is used for preheating the raw material liquid;
the evaporation concentration subsystem is used for carrying out evaporation concentration on the preheated raw material liquid;
and the compression enthalpy-increasing subsystem is used for compressing enthalpy-increasing gas exhausted by the evaporation concentration subsystem, and the gas subjected to compression enthalpy-increasing enters the evaporation concentration subsystem for heat exchange.
2. The evaporative concentration system of claim 1, wherein the pre-heating subsystem comprises: the system comprises a material tank, a first pump, a first preheater and a second preheater;
the outlet of the material tank is connected with the inlet of the first pump, the outlet of the first pump is connected with the first inlet of the first preheater, the first outlet of the first preheater is connected with the first inlet of the second preheater, and the first outlet of the second preheater is connected with the inlet of the evaporation concentration subsystem.
3. The evaporative concentration system of claim 2, wherein the evaporative concentration subsystem comprises an evaporator, a first inlet of the evaporator is connected to a first outlet of the second preheater, a first outlet of the evaporator is connected to an inlet of the compression enthalpy addition subsystem, a second inlet of the evaporator is connected to an outlet of the compression enthalpy addition subsystem, a second outlet of the evaporator is connected to a second inlet of the first preheater, and a second outlet of the first preheater is configured to discharge the non-condensable gas.
4. The evaporative concentration system of claim 3, further comprising a vent valve, an inlet of the vent valve being connected to the second outlet of the evaporator, and an outlet of the vent valve being connected to the second inlet of the first preheater.
5. The evaporative concentration system of claim 3, wherein the compression enthalpy addition subsystem includes: the inlet of the gas-liquid separator is connected with the first outlet of the evaporator, the outlet of the gas-liquid separator is connected with the first inlet of the compressor, and the outlet of the compressor is connected with the second inlet of the evaporator.
6. The evaporative concentration system of claim 5, wherein the compression enthalpy addition subsystem further includes a check valve, an inlet of the check valve being connected to an outlet of the compressor, an outlet of the check valve being connected to the second inlet of the evaporator.
7. The evaporative concentration system of claim 5, wherein the evaporative concentration subsystem further comprises: a condensing tank, an electric heater and a second pump; the compression enthalpy-increasing subsystem further comprises a third pump;
the third export of evaporimeter with the access connection of condensate tank, the first export of condensate tank with the third access connection of evaporimeter, the second export of condensate tank with the access connection of third pump, the export of third pump with the second access connection of compressor, the third export of condensate tank with the access connection of second pump, the export of second pump with the second access connection of second preheater, wherein, the second export of second preheater is used for discharging the comdenstion water, the electric heater sets up in the condensate tank.
8. The evaporative concentration system of claim 3, wherein the evaporative concentration subsystem further comprises: the concentrated solution pump comprises a concentrated solution tank and a fourth pump, wherein an inlet of the concentrated solution tank is connected with a fourth outlet of the evaporator, an outlet of the concentrated solution tank is connected with an inlet of the fourth pump, a first outlet of the fourth pump is used for discharging concentrated solution, and a second outlet of the fourth pump is connected with a fourth inlet of the evaporator.
9. The evaporative concentration system of claim 5, further comprising a controller communicatively coupled to the preheat subsystem, the evaporative concentration subsystem, and the compression enthalpy addition subsystem.
10. The evaporative concentration system of claim 9, wherein the plurality of pipes of the compressor are respectively provided with an on-off valve and a flow meter, the flow meter sends a signal to the controller, and the controller controls the on-off valve to be opened according to the signal.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220033188.XU CN216986314U (en) | 2022-01-07 | 2022-01-07 | Evaporation concentration system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220033188.XU CN216986314U (en) | 2022-01-07 | 2022-01-07 | Evaporation concentration system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216986314U true CN216986314U (en) | 2022-07-19 |
Family
ID=82388288
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202220033188.XU Active CN216986314U (en) | 2022-01-07 | 2022-01-07 | Evaporation concentration system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN216986314U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116206795A (en) * | 2023-01-04 | 2023-06-02 | 中国原子能科学研究院 | Method for starting radioactive waste liquid treatment system |
-
2022
- 2022-01-07 CN CN202220033188.XU patent/CN216986314U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116206795A (en) * | 2023-01-04 | 2023-06-02 | 中国原子能科学研究院 | Method for starting radioactive waste liquid treatment system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN216986314U (en) | Evaporation concentration system | |
| CN204034286U (en) | Board-like mechanical vapour recompression evaporator | |
| CN114367121A (en) | Evaporation concentration system | |
| CN104258583A (en) | MVR evaporator and evaporation method | |
| CN116116023A (en) | Evaporation concentration system | |
| CN217354498U (en) | Steam turbine exhaust steam condensing system based on plate heat exchanger | |
| CN219449369U (en) | Skid-mounted high-power concentrated solution treatment device | |
| CN201373695Y (en) | Combined secondary steam heat energy recovery device for heat pipe phase change heat exchanger of combined heat pump | |
| CN208457934U (en) | Slag waste water residual heat recycles energy saver | |
| CN201373699Y (en) | Combined secondary steam heat energy recovery device for heat pipe phase change heat exchanger of mechanical compression heat pump | |
| CN107857323A (en) | The apparatus and method handled with reference to MVR garbage percolation concentrate | |
| CN104211552B (en) | The device of normal hexane is refined in mixed vegetable oil | |
| CN207918475U (en) | The device that garbage percolation concentrate is handled in conjunction with MVR | |
| CN106186132A (en) | Low cost power plant zeroth order value waste water evaporation and concentration processing system and method | |
| CN101870502B (en) | Space water treatment vaporization system | |
| CN201373698Y (en) | Combined secondary steam heat energy recovery device for conventional phase change heat exchanger of combined heat pump | |
| CN106629937A (en) | Waste water processing technology and system | |
| CN214512756U (en) | Heat pump double-effect evaporation concentration system utilizing high-level heat | |
| CN219423736U (en) | Multistage MVR evaporation economizer of zinc sulfate monohydrate sled dress | |
| CN213707792U (en) | MVR waste water is secondary steam circulating device for evaporation equipment | |
| CN204125400U (en) | The device of normal hexane is refined in mixed vegetable oil | |
| CN114856734B (en) | Steam turbine exhaust steam condensing system based on plate heat exchanger | |
| CN214512757U (en) | Multi-connected heat pump evaporation concentration system based on heat balance principle | |
| CN220939129U (en) | Waste acid concentration device | |
| CN220939130U (en) | Concentrated spent acid joins in marriage sour device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |