CN115523141A - Vortex tube vapor recompression device - Google Patents
Vortex tube vapor recompression device Download PDFInfo
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- CN115523141A CN115523141A CN202211159620.0A CN202211159620A CN115523141A CN 115523141 A CN115523141 A CN 115523141A CN 202211159620 A CN202211159620 A CN 202211159620A CN 115523141 A CN115523141 A CN 115523141A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04C—ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT MACHINES FOR LIQUIDS; ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT PUMPS
- F04C18/00—Rotary-piston pumps specially adapted for elastic fluids
- F04C18/08—Rotary-piston pumps specially adapted for elastic fluids of intermeshing-engagement type, i.e. with engagement of co-operating members similar to that of toothed gearing
- F04C18/12—Rotary-piston pumps specially adapted for elastic fluids of intermeshing-engagement type, i.e. with engagement of co-operating members similar to that of toothed gearing of other than internal-axis type
- F04C18/126—Rotary-piston pumps specially adapted for elastic fluids of intermeshing-engagement type, i.e. with engagement of co-operating members similar to that of toothed gearing of other than internal-axis type with radially from the rotor body extending elements, not necessarily co-operating with corresponding recesses in the other rotor, e.g. lobes, Roots type
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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
- B01D1/30—Accessories for evaporators ; Constructional details thereof
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/30—Accessories for evaporators ; Constructional details thereof
- B01D1/305—Demister (vapour-liquid separation)
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04C—ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT MACHINES FOR LIQUIDS; ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT PUMPS
- F04C29/00—Component parts, details or accessories of pumps or pumping installations, not provided for in groups F04C18/00 - F04C28/00
- F04C29/12—Arrangements for admission or discharge of the working fluid, e.g. constructional features of the inlet or outlet
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04C—ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT MACHINES FOR LIQUIDS; ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT PUMPS
- F04C29/00—Component parts, details or accessories of pumps or pumping installations, not provided for in groups F04C18/00 - F04C28/00
- F04C29/12—Arrangements for admission or discharge of the working fluid, e.g. constructional features of the inlet or outlet
- F04C29/124—Arrangements for admission or discharge of the working fluid, e.g. constructional features of the inlet or outlet with inlet and outlet valves specially adapted for rotary or oscillating piston pumps
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
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- General Engineering & Computer Science (AREA)
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- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
A vortex tube vapor recompression device comprises a three-phase mixed reaction device, a vapor recompression device and a condensate water device. The vortex temperature separation effect is adopted to improve the energy efficiency, and a series of functions including mother liquor heating, mother liquor concentration and crystallization, steam-water separation and slurry output can be completed under the conditions that primary steam is insufficient or no steam is supplied and secondary steam is low in quality. The requirement on steam power source is not high, a centrifugal compressor with high manufacturing cost can be omitted, and a Roots compressor with low rotating speed and large pressure difference is selected, so that the realization of the process can be met. The problems of severe operating conditions and difficult control of the conventional MVR equipment are solved, and the evaporation concentration (crystallization) device which has higher benefit under the environment without steam supply and weak vacuum is provided, so that the control and operation difficulty is reduced.
Description
Technical Field
The invention belongs to the technical field of chemical engineering, relates to comprehensive utilization of evaporation concentration (crystallization) of a mother liquor treatment process, and relates to a vortex tube vapor recompression device.
Background
A vortex tube, also known as a Ranque-Hilsch tube, has an inlet for compressed air and two outlets for automatically separating cold and hot air. Simple structure, low price, and is industrially applied to various cooling scenes in a large quantity. The compressed gas expands in the nozzle, entering the vortex tube tangentially at high velocity. When the airflow rotates at high speed in the vortex tube, the airflow is separated into two parts of airflow, the central temperature is low, and the outer layer temperature is high. The vortex tube is the reverse design of the hot and cold ports, with cold air coming out from the left and hot air coming out from the right. There is also a design with the same direction of cold and heat, but the separation efficiency is much lower.
The direct contact type heat exchange refers to a process of directly contacting a medium and transferring heat, and is not limited by a solid wall surface, so that the heat transfer efficiency is higher, the contact area between the media is increased, the equipment structure is simplified, and the heat exchange process is rapid and efficient. The direct contact type heat exchange of the steam and the water is divided into the following steps according to the movement and contact modes of the steam and the water: the spraying, bead type, film type and bubble type involve the growth and separation process of bubbles, and are widely used in many industrial devices such as heat exchangers, electronic cooling, chemical processing, sewage treatment and the like, and the process is more complicated due to the phase change process.
Three common evaporative concentration crystallization equipment processes are Thermal Vapor Recompression (TVR), multiple Effect technology (MEE), and Mechanical Vapor Recompression (MVR). In order to further improve the energy efficiency, the processes are combined, such as a 2R two-stage compression technology, and the quality of secondary steam is improved under the combined action of a mechanical compressor and a heat pump.
The core of evaporative crystallization is to increase the amount of evaporated water in unit time, i.e. the evaporation rate, and to quickly realize the process from low concentration to high concentration. Therefore, the steam quality needs to be kept high during the operation of the equipment, the effect of the cyclic heating is maintained, and the existing process method also surrounds the core. In particular, vacuum crystallization, also known as vacuum adiabatic cooling crystallization, is a crystallization method in which a solution is flash evaporated under vacuum and adiabatically cooled. Vacuum crystallization essentially relies on both concentration and cooling to produce supersaturation for crystallization. The flash principle is utilized, the pressure is reduced when the thermodynamic equilibrium state is changed to the next thermodynamic equilibrium state, part of sensible heat is released, the excessive heat is absorbed in the form of latent heat, and water is flashed into steam.
In order to control the overall vacuum degree and evaporant temperature and maintain a high evaporation rate, the process equipment in the prior art inevitably enables a main structure to have the characteristics of large diameter and height, and is usually arranged in a multi-layer structure factory building with the height of more than 20 meters.
Disclosure of Invention
The invention aims to provide a vortex tube vapor recompression device which is used for reducing the severe requirements of an evaporative crystallization process on the quality of secondary vapor and a vacuum environment, provides a new scheme for rapid evaporation in a weak vacuum environment without vapor supply, adopts a vortex temperature separation effect, simplifies an evaporative concentration crystallization process, improves energy efficiency, reduces the difficulty of control and operation, can be arranged in a single-layer factory building, and reduces scale and cost.
The technical scheme of the invention is as follows:
comprises a three-phase mixing reaction device, a steam recompression device and a condensate water device. The three-phase mixing reaction device comprises a mother liquor storage tank, a mother liquor delivery pump, a plate heat exchanger, a three-phase tank, a tank body liquid level meter, industrial monitoring, a tank body pressure transmitter, a discharge screw pump, a feed back valve, a discharge valve and a connecting pipeline, wherein an outlet flange at the bottom of the mother liquor storage tank and a pump inlet of the mother liquor delivery pump pass through a pipeline and are connected by flanges, an outlet of the mother liquor delivery pump and a feed inlet of the plate heat exchanger pass through a pipeline and are connected by flanges, a discharge outlet of the plate heat exchanger and a tank top feed inlet of the three-phase tank pass through a pipeline and are connected by flanges, a tank bottom discharge outlet of the three-phase tank and a pump inlet of the discharge screw pump pass through a pipeline and are connected by flanges, the outlet of the discharge screw pump and the feed back valve pass through a tee joint and are connected by flanges, the feed back valve and a feed back port of a side wall of the three-phase tank pass through a pipeline and are connected by flanges, the discharge valve is connected outside the system, the tank body liquid level meter and the side wall of the three-phase tank pass through flanges, the industrial monitoring and the tank body pressure transmitter is fixed at the top middle position of the three-phase tank by flanges.
The steam recompression device comprises a three-phase groove, a steam mixer, a vortex tube, a superheating cavity, a hot end pressure transmitter, a hot end temperature transmitter, an ejector, a steam-water separation tank, a overpressure valve, a Roots compressor, a cold end working hand valve, a cold end exhaust hand valve and a connecting pipeline, wherein a tank top exhaust port of the three-phase groove is connected with a suction port of the ejector through a pipeline and a flange, a discharge port of the ejector is connected with an air inlet at the top of the steam-water separation tank through a pipeline and a flange, an exhaust port at the top of the steam-water separation tank is in three-way connection with an air inlet of the Roots compressor and the overpressure valve through a pipeline and a flange, the overpressure valve connection system is used for emptying outside, the gas outlet of the Roots compressor is connected with the gas inlet of the vortex tube through a tube bank, the hot end gas outlet of the vortex tube is connected to the overheating cavity through the tube bank, the overheating cavity is connected with the gas inlet of the steam mixer through a pipeline and a flange, the cold end gas outlet of the vortex tube is connected to the working flow inlet of the ejector through the tube bank, a cold end working hand valve is arranged between the cold end of the vortex tube and the ejector, a cold end exhaust hand valve communicated with the atmosphere is arranged on the upstream of the cold end working hand valve through a tee joint, and a hot end pressure transmitter and a hot end temperature transmitter are fixed on the overheating cavity through threads.
The condensed water device comprises a plate type heat exchanger, a steam-water separation tank, a condensed water pump, a circulating water control valve, a heating water inlet thermometer, a heating water outlet thermometer, a liquid level control valve, a distribution plate and a connecting pipeline, wherein a water outlet of the steam-water separation tank is connected with a pump inlet of the condensed water pump through a pipeline and a flange, a pump outlet of the condensed water pump is connected with the circulating water control valve through a pipeline and a flange, the circulating water control valve is connected with a water inlet of the plate type heat exchanger through a pipeline and a flange, a water outlet of the plate type heat exchanger is connected with a water return port of the steam-water separation tank and the liquid level control valve through a pipeline and a flange in a three-way manner, the heating water inlet thermometer and the heating water outlet thermometer are respectively fixed on a water inlet pipeline and a water outlet pipeline of the plate type heat exchanger through threads, the liquid level control valve is connected outside the system, a water return port of the steam-water separation tank is connected with the distribution plate through a flange, and the distribution plate is fixed on the lower side in the steam-water separation tank through a support.
The optimal set value can be found by evaluating the final water discharge and the water discharge temperature of the system and verifying the liquid level and the vacuum degree of the three-phase tank and the factors such as the opening degree of the hot end adjusting hand valve, the temperature and the pressure of the overheating cavity and the like.
The invention perfects the application of the evaporation concentration crystallization process in the weak vacuum environment, improves the energy efficiency by adopting the vortex temperature separation effect, and can complete a series of functions including mother liquor heating, mother liquor concentration (crystallization), steam-water separation and slurry output under the conditions of insufficient primary steam supply (or no steam supply) and low secondary steam quality. The requirement on steam power source is not high, a centrifugal compressor with high manufacturing cost can be omitted, and a Roots compressor with low rotating speed and large pressure difference is selected, so that the realization of the process can be met. Therefore, the beneficial effects of the invention are as follows: the problems of severe operating conditions and difficult control of the conventional MVR equipment are solved, the evaporation concentration (crystallization) device which has higher benefit under the environment without steam supply and weak vacuum is provided, and the difficulty of control and operation is reduced.
Drawings
Fig. 1 is a schematic structural view of a vortex tube vapor recompression device.
FIG. 2 is a schematic diagram of vortex tube operation.
Fig. 3 is a schematic diagram of the ejector.
Fig. 4 is a schematic diagram of the operation of a steam mixer.
In the figure: 1-mother liquor storage tank, 2-mother liquor delivery pump, 3-plate heat exchanger, 4-three-phase tank, 5-steam mixer, 6-tank level meter, 7-industrial monitoring, 8-tank pressure transmitter, 9-vortex tube, 10-hot end regulating hand valve, 11-superheating chamber, 12-hot end pressure transmitter, 13-hot end temperature transmitter, 14-ejector, 15-steam-water separation tank, 16-steam-water level meter, 17-condensate pump, 18-circulating water control valve, 19-heating water inlet thermometer, 20-heating water outlet thermometer, 21-liquid level control valve, 22-distribution plate, 23-secondary steam pressure transmitter, 24-overpressure valve, 25-roots compressor, 26-discharge screw pump, 27-return valve, 28-discharge valve, 29-cold end working hand valve, 30-cold end exhaust hand valve.
Detailed Description
The invention will be further explained with reference to the following embodiments in the drawings.
FIG. 1 shows: vortex tube vapor recompression device, including three-phase mixed reaction unit, 3 parts altogether of vapor recompression device and comdenstion water device, the material gets into three-phase mixed reaction unit, and vapor recompression device handles the steam that three-phase mixed reaction unit produced for steam circulates in three-phase mixed reaction unit, and partial steam passes through the comdenstion water device and arranges outside the system.
The three-phase mixing reaction device comprises a mother liquor storage tank 1, a mother liquor delivery pump 2, a plate heat exchanger 3, a three-phase tank 4, a tank body liquid level meter 6, an industrial monitor 7, a tank body pressure transmitter 8, a discharging screw pump 26, a material return valve 27, a discharging valve 28 and a connecting pipeline. An outlet flange at the bottom of a mother liquid storage tank 1 and a pump inlet of a mother liquid conveying pump 2 are connected through a pipeline and a flange, a pump outlet of the mother liquid conveying pump 2 and a feed inlet of a plate heat exchanger 3 are connected through a pipeline and a flange, a discharge outlet of the plate heat exchanger 3 and a tank top feed inlet of a three-phase tank 4 are connected through a pipeline and a flange, a tank bottom discharge outlet of the three-phase tank 4 and a pump inlet of a discharge screw pump 26 are connected through a pipeline and a flange, a pump outlet of the discharge screw pump 26 and a material return valve 27 are connected through a tee joint and a flange, the material return valve 27 and a material return opening of the side wall of the three-phase tank 4 are connected through a pipeline and a flange, the discharge valve 28 is connected outside the system, a tank body liquid level meter 6 and the side wall of the three-phase tank 4 are connected through a flange, an industrial monitor 7 and a tank body pressure transmitter 8 are fixed at the top middle position of the three-phase tank 4 through a flange.
The vapor recompression device comprises a three-phase groove 4, a vapor mixer 5, a vortex tube 9, a superheat chamber 11, a hot end pressure transmitter 12, a hot end temperature transmitter 13, an ejector 14, a vapor-water separation tank 15, a overpressure valve 24, a roots compressor 25, a cold end working hand valve 29, a cold end exhaust hand valve 30 and a connecting pipeline. The exhaust port at the top of the tank of the three-phase tank 4 is connected with the suction port of the ejector 14 through a pipeline and a flange, the exhaust port at the top of the ejector 14 is connected with the air inlet at the top of the steam-water separation tank 15 through a pipeline and a flange, the exhaust port at the top of the steam-water separation tank 15 is connected with the air inlet of the Roots compressor 25 through a pipeline and a flange in a three-way manner, the overpressure valve 24 is connected with the outside of the system and exhausted, the air outlet of the Roots compressor 25 is connected with the air inlet of the vortex tube 9 through a tube bank, the hot end air outlet of the vortex tube 9 is connected to the overheating chamber 11 through a tube bank, the overheating chamber 11 is connected with the air inlet of the steam mixer 5 through a pipeline and a flange, similarly, the cold end air outlet of the vortex tube 9 is connected with the working flow inlet of the ejector 14 through a tube bank, a cold end working hand valve 29 is arranged between the vortex tube 9 and the ejector 14, a cold end exhaust hand valve 30 is arranged at the upstream of the cold end working hand valve 29 through a three-way and communicated with the atmosphere, and the hot end temperature transmitter 12 and the hot end temperature 13 are fixed on the overheating chamber 11 through threads.
The condensate device comprises a plate type heat exchanger 3, a steam-water separation tank 15, a condensate pump 17, a circulating water control valve 18, a heating water inlet thermometer 19, a heating water outlet thermometer 20, a liquid level control valve 21, a distribution plate 22 and a connecting pipeline. The water outlet of the steam-water separating tank 15 is connected with the pump inlet of the condensed water pump 17 through a pipeline and a flange, the pump outlet of the condensed water pump 17 is connected with the circulating water control valve 18 through a pipeline and a flange, the circulating water control valve 18 is connected with the water inlet of the plate type heat exchanger 3 through a pipeline and a flange, the water outlet of the plate type heat exchanger 3 is connected with the water return port of the steam-water separating tank 15 and the liquid level control valve 21 through a pipeline and a flange in a three-way manner, a heating water inlet thermometer 19 and a heating water outlet thermometer 20 are respectively fixed on the water inlet pipeline and the water outlet pipeline of the plate type heat exchanger 3 through threads, the liquid level control valve 21 is connected outside the system, the water return port of the steam-water separating tank 15 is connected with a distribution plate 22 through a flange, and the distribution plate 22 is fixed on the lower side in the steam-water separating tank 15 through a bracket.
The working process and principle are as follows:
before operation, checking the station of the valve: the hot end regulating hand valve 10 is opened to the maximum, the circulating water control valve 18 and the liquid level control valve 21 are closed, the overpressure valve 24 is closed, the material return valve 27 is opened, the discharge valve 28 is closed, the cold end exhaust hand valve 30 is opened, and the cold end working hand valve 29 is closed.
The water and electricity condition of the roots compressor 25 is provided, the roots compressor 25 is started at the lowest frequency, and the working condition is as follows: the hot end of the vortex tube 9 outputs hot air (the temperature and the pressure of the overheating cavity 11 are increased), the temperature of the cold end of the vortex tube 9 is reduced, cold air is exhausted to the atmosphere, and the three-phase tank 4-steam-water separator is slowly changed into a weak vacuum environment.
Observing until the indication values of the hot end pressure transmitter 12, the hot end temperature transmitter 13 and the tank body pressure transmitter 8 change slowly, and working conditions are as follows: the temperature of the three-phase tank 4 and the steam-water separation tank 15 rises to more than 80 ℃, the heating source is hot-end air discharged from the steam mixer 5, cold-end air is exhausted, and the air pressure in the three-phase tank 4-the steam-water separation tank 15 maintains weak vacuum.
The mother liquor delivery pump 2 is started, the mother liquor enters the three-phase tank 4 through the plate heat exchanger 3, the discharge screw pump 26 is started, and the mother liquor circulates in the three-phase tank 4 through the material return valve 27, so that the working condition is as follows: the system has no condensed water, at the moment, the plate heat exchanger 3 does not work, a small amount of mother liquor is evaporated in the three-phase tank 4, a weak vacuum environment is compensated and slowly becomes micro-positive pressure, the heating source is air-steam mixed gas, the hot end of the vortex tube 9 is heated in the process of mixed gas pressurization circulation, the mixed gas is in a gaseous state all the time, the cold end of the vortex tube is cooled, the discharged mixed gas has a fogging phenomenon, the mixed gas is formed by cooling and condensing the steam in the mixed gas, the fogging phenomenon of waiting for the exhaust of the cold end of the vortex tube 9 is stable, and at the moment, the air-steam mixed gas is mainly steam.
The circulating water control valve 18 is opened, the cold-end working hand valve 29 is opened, and the cold-end exhaust hand valve 30 is closed. The working conditions are as follows: high-speed fluid at the cold end of the vortex tube 9 enters the ejector 14, is mixed with steam of the three-phase groove 4 in the ejector 14 to form saturated steam with water, enters the steam-water separation tank 15, passes through the distribution plate 22, reduces the temperature of the steam-water separation tank 15, and forms a large amount of condensed water.
The indication value of the steam-water level meter 16 exceeds 50%, the circulating water pipe can be ensured to be full of condensed water, the condensed water pump 17 is started, and the working frequency of the Roots compressor 25 is improved. The working conditions are as follows: the inlet-outlet pressure difference of the Roots compressor 25 is increased, the temperature difference between the hot end and the cold end of the vortex tube 9 is further increased, the latent heat of the hot-end superheated steam is increased, the water quantity of the cold-end wet saturated steam is increased, and the plate heat exchanger 3 starts to take effect. The stable working process of the system:
(1) the medium of the vortex tube 9, the overheating cavity 11 and the steam mixer 5 is high-pressure and overheated steam (above 150 ℃), the overheated steam micro-bubble releases latent heat in mother liquor, water is evaporated on the bubble interface, the volume is enlarged, local steam and water are co-boiled, the kinetic energy of the steam is transferred to drive the mother liquor to flow, and crystal particles are not easy to settle; the liquid level of the three-phase tank 4 is adjusted, the gas production rate of steam and water transpiration is observed through an industrial monitor 7, and the optimal liquid level when the evaporation rate is maximum is determined.
(2) Injecting high-speed fluid at the cold end of the vortex tube 9, extracting saturated steam generated after superheated steam and mother liquor in the three-phase tank 4 are mixed, so that the three-phase tank 4 maintains weak vacuum and accelerates evaporation, wherein the vacuum degree is related to the flow of the fluid at the cold end; the evaporation capacity and the vacuum degree of the three-phase tank 4 are changed by adjusting the opening degree of the hot end adjusting hand valve 10 and changing the temperature difference and the flow ratio of the cold end and the hot end of the vortex tube 9.
(3) The medium is wet saturated steam with relatively low temperature (90-100 ℃ under the negative pressure condition) and is in direct contact with condensate return water (40-60 ℃) with lower temperature on a distribution plate 22 for heat exchange, the yield of the condensate is increased, and a liquid level control valve 21 is opened to stabilize the liquid level of the steam-water separation tank 15.
The liquid level and the vacuum degree of the three-phase tank 4 can be verified by evaluating the final water discharge and the water discharge temperature of the system, and the optimum set value can be found by adjusting the opening degree of the hand valve 10 and the temperature and the pressure of the overheating cavity 11 at the hot end.
Particularly, under the condition of no steam supply, the method adopts the following steps to start the machine:
(1) before operation, checking the station of the valve: the hot end regulating hand valve 10 is opened to the maximum, the circulating water control valve 18 and the liquid level control valve 21 are closed, the overpressure valve 24 is closed, the material return valve 27 is opened, the discharge valve 28 is closed, the cold end exhaust hand valve 30 is opened, and the cold end working hand valve 29 is closed;
(2) the water and electricity conditions of the Roots compressor 25 are met, and the Roots compressor 25 is started at the lowest frequency;
(3) observing, starting a mother liquor conveying pump 2 until the indication values of the hot end pressure transmitter 12, the hot end temperature transmitter 13 and the tank body pressure transmitter 8 are slowly changed, enabling the mother liquor to enter the three-phase tank 4 through the plate heat exchanger 3, starting a discharging screw pump 26, and enabling the mother liquor to circulate in the three-phase tank 4 through a material returning valve 27;
(4) opening the circulating water control valve 18, opening the cold-end working hand valve 29 and closing the cold-end exhaust hand valve 30;
(5) and the indication value of the steam-water liquid level meter 16 is observed to exceed 50%, the circulating water pipe can be ensured to be full of condensed water, the condensed water pump 17 is started, the working frequency of the Roots compressor 25 is improved, and the device stably operates.
When the device is in operation, the hot end of the vortex tube 9, the overheating cavity 11 and the steam mixer 5 are used, the medium is high-pressure and overheated steam (above 150 ℃), the microbubbles of the overheated steam release latent heat in mother liquor, the bubble interface evaporates water, the volume is enlarged, local steam and water are co-evaporated, the kinetic energy of the steam is transferred to drive the mother liquor to flow, and crystal particles are not easy to settle.
During the operation of the device, the injection of high-speed fluid at the cold end of the vortex tube 9 extracts saturated steam generated after superheated steam and mother liquor in the three-phase tank 4 are mixed, so that the three-phase tank 4 maintains weak vacuum and the evaporation is accelerated.
When the device stably operates, the cold end of the vortex tube 9, the ejector 14 and the steam-water separation tank 15 have the medium of wet saturated steam with relatively low temperature, the negative pressure condition is 90-100 ℃, the medium and condensate water with lower temperature of 40-60 ℃ are directly contacted with the distribution plate for heat exchange, and a large amount of condensate water is produced.
As shown in fig. 2, the pressurized steam from the screw compressor 25 enters from the inlet of the vortex tube 9, and due to the internal structure, when the pressurized steam rotates at a high speed in the vortex tube, the pressurized steam is separated into cold and hot air flows, the center temperature is low, the outer layer temperature is high, and the hot end adjusting hand valve 10 is adjusted to allow the warmed superheated steam to flow from the superheating cavity 11 at the left side (hot end) to the steam mixer 5, and also allow the cooled wet saturated steam to flow from the right side (cold end) to the ejector 14 through the cold end working hand valve 29.
FIG. 3 shows: the wet saturated steam output from the cold end of the vortex tube 9 is used as an injection flow of the injector 14 and forms high-speed airflow after passing through a convergent-divergent nozzle of the injector 14, the flash evaporation saturated steam of the three-phase tank 4 is used as an injected flow, high vacuum is formed at an outlet of the nozzle due to injection effect, and the steam of the three-phase tank 4 is pumped away and mixed into uniform wet saturated steam.
FIG. 4 shows: superheated steam output from the hot end of the vortex tube 9 enters the steam mixer 4 and is sprayed into the mother liquor through the steam mixer 4, and the steam microbubbles generated due to the tiny inclined holes on the wall plate of the steam mixer 4 have strong injection effect on surrounding cold water to form rotating water vapor, so that the liquid level of the mother liquor is controlled, the microbubbles of the superheated steam are separated from the liquid level before latent heat is completely released and enter the gas phase of the three-phase tank 4, and the steam is not subjected to complete heat exchange with the cold water.
Claims (2)
1. Vortex tube vapor recompression device, its characterized in that: the system comprises a three-phase mixed reaction device, a steam recompression device and a condensate water device, wherein mother liquor enters the three-phase mixed reaction device, the steam recompression device treats steam generated by the three-phase mixed reaction device, the steam is circulated in the three-phase mixed reaction device, and part of the steam is discharged out of the system through the condensate water device;
the three-phase mixing reaction device comprises a mother liquor storage tank, a mother liquor conveying pump, a plate heat exchanger, a three-phase tank, a tank body liquid level meter, industrial monitoring, a tank body pressure transmitter, a discharging screw pump, a material return valve, a discharging valve and a connecting pipeline, wherein an outlet flange at the bottom of the mother liquor storage tank is connected with a pump inlet of the mother liquor conveying pump through a pipeline and a flange;
the steam recompression device comprises a three-phase groove, a steam mixer, a vortex tube, a superheating cavity, a hot end pressure transmitter, a hot end temperature transmitter, an ejector, a steam-water separation tank, a overpressure valve, a Roots compressor, a cold end working hand valve, a cold end exhaust hand valve and a connecting pipeline, wherein a tank top exhaust port of the three-phase groove is connected with a suction port of the ejector through a pipeline and a flange, an exhaust port of the ejector is connected with an air inlet at the top of the steam-water separation tank through a pipeline and a flange, the exhaust port at the top of the steam-water separation tank is connected with an air inlet of the Roots compressor and the overpressure valve through a pipeline and a flange in a three-way manner, the outside of the overpressure valve connection system is exhausted, an air outlet of the Roots compressor is connected with an air inlet of the vortex tube through a tube bank, a hot end of the vortex tube is connected with the superheating cavity through a tube bank, the superheating cavity is connected with the air inlet of the steam mixer through a pipeline and a flange, the cold end air outlet of the vortex tube is connected with a working flow inlet of the ejector through a tube bank, the cold end of the vortex tube is connected with the cold end working hand valve, the cold end of the vortex tube, the cold end working hand valve, the hot end pressure transmitter and the hot end pressure transmitter are fixed on the hot end of the hot end temperature transmitter through threads.
2. The vortex tube vapor recompression device as recited in claim 1, wherein: the condensed water device comprises a plate type heat exchanger, a steam-water separation tank, a condensed water pump, a circulating water control valve, a heating water inlet thermometer, a heating water outlet thermometer, a liquid level control valve, a distribution plate and a connecting pipeline, wherein a water outlet of the steam-water separation tank is connected with a pump inlet of the condensed water pump through a pipeline and a flange, a pump outlet of the condensed water pump is connected with the circulating water control valve through a pipeline and a flange, the circulating water control valve is connected with a water inlet of the plate type heat exchanger through a pipeline and a flange, a water outlet of the plate type heat exchanger is connected with a water return port of the steam-water separation tank and the liquid level control valve through a pipeline and a flange in a three-way manner, the heating water inlet thermometer and the heating water outlet thermometer are respectively fixed on a water inlet pipeline and a water outlet pipeline of the plate type heat exchanger through threads, the liquid level control valve is connected outside the system, a water return port of the steam-water separation tank is connected with the distribution plate through a flange, and the distribution plate is fixed on the lower side in the steam-water separation tank through a support.
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| CN202211159620.0A CN115523141A (en) | 2022-09-22 | 2022-09-22 | Vortex tube vapor recompression device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117028960A (en) * | 2023-09-27 | 2023-11-10 | 国网江苏省电力有限公司常州供电分公司 | Closed circulation steam generating device with heat storage function |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117028960A (en) * | 2023-09-27 | 2023-11-10 | 国网江苏省电力有限公司常州供电分公司 | Closed circulation steam generating device with heat storage function |
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