CN210825502U - Scale inhibition and scale removal system for gypsum magnetic crystal seeds and evaporative crystallization system - Google Patents
Scale inhibition and scale removal system for gypsum magnetic crystal seeds and evaporative crystallization system Download PDFInfo
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- CN210825502U CN210825502U CN201920935196.1U CN201920935196U CN210825502U CN 210825502 U CN210825502 U CN 210825502U CN 201920935196 U CN201920935196 U CN 201920935196U CN 210825502 U CN210825502 U CN 210825502U
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Abstract
The utility model relates to a scale inhibition and scale removal technical field provides gypsum magnetism crystal seed scale inhibition and scale removal system and evaporation crystal system, and wherein, gypsum magnetism crystal seed scale inhibition and scale removal system includes crystal seed circulation subsystem, crystal seed circulation subsystem passes through the pipeline and is connected with the treatment facility and forms crystal seed circulation circuit, crystal seed circulation subsystem includes magnetic field generating device, magnetic field generating device is used for the magnetization to flow through magnetic field generating device's gypsum crystal seed is in order to form gypsum magnetism crystal seed. The evaporative crystallization system comprises a crystallizer and a seed crystal circulation subsystem, wherein the seed crystal circulation subsystem is connected with the crystallizer through a pipeline to form a seed crystal circulation loop. The utility model discloses a magnetization seed crystal is to treatment facility scale inhibition and scale removal, and the magnetization seed crystal circulation flow between treatment facility and seed crystal circulation subsystem stably keeps the magnetization state of seed crystal, and the reinforcing antiscale descaling effect.
Description
Technical Field
The utility model relates to a scale inhibition and removal technical field especially relates to gypsum magnetic crystal seed scale inhibition and removal system and evaporative crystallization system.
Background
The chemical production process comprises the processes of fluid flowing, heat transfer, mass transfer and the like, the chemical process needs the matching of chemical equipment, the problems of scaling, blockage and the like easily occur in the long-term operation of the chemical equipment, the problems of scaling, blockage and the like not only influence the operation efficiency of the equipment, but also have potential safety hazards.
Equipment fouling refers to the accumulation of a layer of solid material in which components or impurities in the fluid gradually crystallize or adsorb on surfaces in contact with the fluid, wherein heat exchange equipment fouling is widespread in various heat transfer processes.
According to the investigation of various types of heat transfer and heat exchange equipment in industrial production, the problems of fouling of different degrees exist. Fouling of heat exchange surfaces is a very serious production problem that affects the rational design and normal operation of heat exchange equipment. Dirt on the heat exchange surface is usually in the form of solid mixture, is a poor heat conductor, has low heat conductivity coefficient and seriously influences the heat exchange efficiency of the equipment.
Crystallization or scaling on the heat exchange surface not only deteriorates the heat transfer performance of the heat exchange equipment and increases the consumption of metal materials, but also reduces the flow cross section of fluid after the dirt layer is thickened, increases the fluid resistance, increases the power of a pump or a fan for conveying the fluid and increases the running energy consumption of the equipment.
In addition, the accumulation of dirt on the heat exchange surface often causes local uneven heating to cause mechanical performance reduction, causes accidents, also causes local corrosion and even perforation of the heat exchange surface, and seriously threatens the safe operation of chemical equipment.
Particularly, in the evaporative crystallization process, the rate of the evaporative crystallization process is mainly controlled by the heat transfer rate, and in the actual production process, the production efficiency is greatly reduced due to the formation of dirt at the heat exchange part of the crystallizer, and sometimes the production can be recovered to be normal only by stopping production of cleaning equipment, so that great inconvenience is brought to the production, and energy consumption, reduction of the production capacity of the equipment and increase of the production cost are caused at the same time.
In the high-salinity wastewater zero-discharge process, the chemical agent softening treatment is needed in the advanced treatment of the high-salinity wastewater, the treatment process needs to be stopped, the flow is complex, the time consumption is long, and the cost is high; the traditional scale inhibition and removal method generally aims at specific calcium sulfate scale, has poor removal effect on other components in the scale, is limited in use range, causes corrosion of equipment to different degrees, shortens the service life of the equipment, and has frequent equipment cleaning and complex cleaning work.
SUMMERY OF THE UTILITY MODEL
Technical problem to be solved
The utility model discloses aim at solving one of the technical problem that exists among prior art or the correlation technique at least: (1) the traditional scale inhibition and removal work cannot be carried out on line in real time, and needs to be stopped for cleaning, so that production stagnation is caused, equipment is corroded in different degrees, the service life of the equipment is shortened, the equipment is cleaned frequently, and the cleaning work is complicated; (2) for the zero-discharge process of the high-salinity wastewater, the chemical agent softening treatment is needed for the advanced treatment of the high-salinity wastewater, the cost is high, the chemical agent is used for removing specific components, and the application range is limited.
(II) technical scheme
In order to solve the technical problem, the utility model provides a gypsum magnetism crystal seed scale inhibition and scale removal system, including the seed crystal circulation subsystem, the seed crystal circulation subsystem passes through the pipeline and is connected formation seed crystal circulation circuit with pending treatment facility, the seed crystal circulation subsystem includes magnetic field generating device, magnetic field generating device is used for the magnetization to flow through magnetic field generating device's gypsum seed crystal is in order to form gypsum magnetism seed crystal.
In some embodiments, the seed circulation subsystem further comprises a seed container and a seed circulation pump, both connected to the seed circulation loop.
In some technical solutions, the magnetic field generating device generates a strong alternating magnetic field, and the magnetic field strength generated by the magnetic field generating device ranges from 5000-50000 gauss.
In some technical solutions, the magnetic field generating device includes an induction power supply, an electromagnetic induction coil, a magnetic field receiving assembly, a fluid conveying pipeline and a cooling circulation system, the induction power supply is that alternating current is introduced into the electromagnetic induction coil, the electromagnetic induction coil is wound around the fluid conveying pipeline, the magnetic field receiving assembly is arranged in the fluid conveying pipeline, the fluid conveying pipeline is connected with a pipeline of the seed crystal circulation loop, the electromagnetic induction coil is set as a hollow spiral pipe, and the electromagnetic induction coil is connected with the cooling circulation system.
In some technical schemes, the device further comprises a seed crystal slurry separation and extraction subsystem, wherein the seed crystal slurry separation and extraction subsystem is connected to the device to be processed and comprises a delayer, a seed crystal thickener, a settler, a first solid-liquid separator and a first mother liquid buffer tank, the delayer is connected to the device to be processed, a seed crystal slurry outlet of the delayer, the seed crystal thickener, the settler and the first solid-liquid separator are sequentially connected, a mother liquid outlet of the delayer, a mother liquid outlet of the seed crystal thickener, a mother liquid outlet of the settler and a mother liquid outlet of the first solid-liquid separator are all connected to the device to be processed and/or the first mother liquid buffer tank, and the first mother liquid buffer tank is connected to the device to be processed.
The utility model also provides an evaporative crystallization system, including the crystallizer, include seed crystal circulation subsystem, seed crystal circulation subsystem pass through the pipeline with the crystallizer is connected and is formed seed crystal circulation circuit.
In some technical schemes, the adding concentration of the gypsum seed crystal in the crystallizer is set to be 20-25 g/L, and the discharging concentration of the gypsum seed crystal in the crystallizer is set to be 30-40 g/L.
In some technical schemes, the crystallizer is further connected with a salt slurry separation and extraction subsystem, the salt slurry separation and extraction subsystem comprises a salt slurry thickener, a second solid-liquid separator and a second mother liquid buffer tank, the salt slurry thickener is connected with the crystallizer, a salt slurry outlet of the salt slurry thickener is connected with the second solid-liquid separator, a slurry outlet of the salt slurry thickener and a slurry outlet of the second solid-liquid separator are connected with the second mother liquid buffer tank and/or the crystallizer, and the second mother liquid buffer tank is connected with the crystallizer.
In some technical schemes, the steam compression subsystem comprises a compressor, a gas-liquid separator, a water tank, an oil supply pump and an oil tank,
a steam outlet of the crystallizer is connected with an inlet of the compressor, a steam outlet of the compressor is connected with the gas-liquid separator, a steam outlet of the gas-liquid separator is connected with the heater, a liquid outlet of the gas-liquid separator is connected with the water tank, and the water tank is connected with an inlet of the compressor;
the oil outlet of the compressor is connected with the oil tank, and the oil tank and the oil inlet of the compressor are connected with the oil supply pump.
In some technical solutions, the crystallizer further comprises a heater and a vapor compression subsystem, a vapor outlet of the crystallizer is connected with the vapor compression subsystem, a heat source outlet of the vapor compression subsystem is connected with a heat source side inlet of the heater, and a cold source side of the heater is connected with the crystallizer to form a crystallization circulation loop.
In some technical schemes, the crystallizer is designed to be in an axial reverse circulation type, the crystallizer comprises an evaporation section, a crystallization section and a salt leg section, a circulation liquid outlet pipe and a demister are arranged in the crystallizer, the circulation liquid outlet pipe extends into the evaporation section, the demister is arranged at the evaporation section and is positioned above the circulation liquid outlet pipe, the crystallization section is provided with a seed crystal sampling port, and the salt leg section is provided with a salt concentration sampling port and a reverse flushing port.
(III) advantageous effects
Compared with the prior art, the utility model has the advantages of it is following:
(1) and gypsum magnetic seed crystals are provided for the equipment to be treated, and circularly flow in the equipment to be treated and the seed crystal circulation subsystem, so that the gypsum seed crystals are continuously kept in a magnetized state, and the scale inhibition and scale removal effects are enhanced. And in the process that the gypsum magnetic seed crystal circulates in the seed crystal circulation subsystem, new gypsum seed crystal is added into the seed crystal circulation subsystem, and the new gypsum seed crystal is magnetized by the gypsum magnetic seed crystal and flows into equipment to be treated after being mixed for scale inhibition and scale removal.
(2) The operation process does not need medicament cost, does not need to be shut down and processed, greatly reduces the scale inhibition and removal cost, and solves the problems that the prior high-salinity wastewater zero-discharge process needs to soften water quality in the early stage, the processing flow is complex, the cost is high and the equipment is corroded.
(3) The crystal seed particle scale inhibition and removal device is suitable for various types of water quality scale inhibition and removal such as calcium sulfate, calcium carbonate and the like, is wide in application range, solves the problem that the traditional crystal seed method scale inhibition and removal only aims at specific calcium sulfate scale, strengthens the scale inhibition and removal efficiency of the crystal seed method, simultaneously expands the scale inhibition and removal range, can effectively remove other scale layer components including calcium carbonate scale, accelerates the removal of the scale layers such as calcium carbonate and the like in the collision process of the crystal seed particles with a heat exchange wall surface due to the existence of the crystal seed particles in an evaporation system, and further improves the removal efficiency of other types of scale layers.
(4) The scale inhibition and descaling device is suitable for evaporation crystallization equipment, can be carried out in real time during the operation of the equipment, greatly reduces the scale formation risk of the evaporation equipment, and solves the problems that the traditional scale inhibition and descaling work cannot be carried out on line in real time, the equipment is frequently cleaned, the cleaning work is complicated, the cleaning cost is high and the like.
(5) And the waste heat of the secondary steam of the crystallizer is recycled, the evaporation equipment is efficient and energy-saving, and the method can be widely applied to the evaporation crystallization process with zero discharge of high-salinity wastewater, and is particularly suitable for the evaporation process with zero discharge of desulfurization wastewater of a power plant.
Drawings
FIG. 1 is a schematic structural view of a preferred embodiment of the gypsum magnetic crystal scale inhibiting and removing system of the present invention;
FIG. 2 is a schematic structural diagram of a preferred embodiment of the evaporative crystallization system of the present invention;
FIG. 3 is a schematic structural diagram of a magnetic field generator of the evaporative crystallization system according to a preferred embodiment of the present invention;
FIG. 4 is a schematic diagram of the internal structure of a preferred embodiment of the seed slurry separation and extraction subsystem of the evaporative crystallization system of the present invention;
FIG. 5 is a schematic diagram of a preferred embodiment of the salt slurry separation and recovery subsystem of the evaporative crystallization system of the present invention;
FIG. 6 is a schematic diagram of a preferred embodiment of the vapor compression subsystem of the evaporative crystallization system of the present invention;
FIG. 7 is a schematic structural view of a preferred embodiment of a crystallizer of the evaporative crystallization system of the present invention;
in the figure, 1, a seed crystal container; 2. a magnetic field generating device; 3. a seed crystal circulating pump; 4. a seed crystal slurry separation and extraction subsystem; 5. an evaporation circulating pump; 6. a salt slurry separation and extraction subsystem; 7. a vapor compression subsystem; 8. a crystallizer; 9. a heater; 10. a condensate tank.
201. A flux concentrating core; 202. a fluid delivery conduit; 203. a pipeline heat-insulating layer; 204. an electromagnetic induction coil; 205. sealing the heat preservation cover; 206. a first regulating valve; 207. a cooling water pump; 208. a cooling circulation water tank; 209. a sewage draining pipeline; 210. a heat exchange coil; 211. a control cabinet; 212. a first pressure sensor; 213. a first temperature sensor; 214. a first flow sensor; 215. a first liquid level sensor; 216. an inductive power supply; 217. a second temperature sensor.
401. A delayer; 402. a seed thickener; 403. a settler; 404. a first solid-liquid separator; 405. a first mother liquor buffer tank.
601. A salt slurry thickener; 602. a second solid-liquid separator; 603. and a second mother liquor buffer tank.
701. A compressor; 702. a gas-liquid separator; 703. an oil tank; 704. a vapor filter; 705. a water tank; 706. a water supply pump; 707. a water supply filter; 708. a second liquid level sensor; 709. a second regulating valve; 710. a third regulating valve; 711. a third temperature sensor; 712. an oil supply pump; 713. and an oil supply filter.
801. An upper cone; 802. a demister; 803. a circulating liquid outlet pipe; 804. an evaporation section; 805. a circulating liquid inlet; 806. a crystallization section; 807. a salt leg section; 808. and (4) backflushing the opening.
Detailed Description
The following detailed description of the embodiments of the present invention is provided with reference to the accompanying drawings and examples. The following examples are intended to illustrate the invention, but are not intended to limit the scope of the invention.
In order to solve the problem of equipment scaling in chemical production, particularly scale inhibition and scaling of high-salinity wastewater zero-discharge system equipment of a power plant, the existing chemical treatment mode is adopted, water softening is needed, the scale removal process is complex and high in cost, and the production progress and the production cost are influenced. The utility model provides a need not to add chemical reagent, need not to shut down, easy and simple to handle and just scale inhibition scale removal system with low costs.
The utility model provides a gypsum magnetism crystal seed scale inhibition and scale removal system combines fig. 1-fig. 7 to show, including the seed crystal circulation subsystem, the seed crystal circulation subsystem passes through the pipeline and is connected formation seed crystal circulation circuit with pending equipment, and the solution that contains the gypsum seed crystal flows in the seed crystal circulation circuit, and the seed crystal circulation subsystem includes magnetic field generating device 2, and magnetic field generating device 2 is used for producing magnetic field, and the magnetic field that magnetic field generating device 2 produced is used for the gypsum seed crystal that the magnetic field generator 2 was flowed through to the magnetization, and the gypsum seed crystal receives the magnetic field effect and forms gypsum magnetism seed crystal at the flow in-process.
The gypsum magnetic crystal seed is acted by a magnetic field to form the gypsum magnetic crystal seed, the gypsum magnetic crystal seed optimizes the crystallization habit relative to the gypsum crystal seed, the gypsum magnetic crystal seed can efficiently induce calcium sulfate in a solution to be attached to the gypsum magnetic crystal seed to form crystals, the calcium sulfate is prevented from being attached to the wall surface of equipment, scaling caused by the fact that the calcium sulfate is attached to the wall surface of the equipment is avoided, and the treatment efficiency of removing the scaling on the wall surface of the equipment to be treated by the gypsum magnetic crystal seed is high. The gypsum magnetic crystal seed can quickly and accurately remove calcium sulfate scale in the solution, solves the problem that the calcium sulfate scale is stubborn and difficult to remove in the prior art, and is especially suitable for the solution with higher content of the calcium sulfate scale, such as desulfurization wastewater, salt-making brine and the like.
Calcium sulfate in the solution is got rid of to gypsum magnetism seed crystal simultaneously, water in the magnetic field generating device magnetization solution simultaneously, magnetic field has changed osmotic pressure and surface tension etc. of water, can make the dirt layer become loose, drop from the wall easily, be used for getting rid of the lower dirt of contents such as calcium carbonate, silica, the dirt of multiple component is got rid of simultaneously, because the existence of seed crystal granule among the vaporization system, the seed crystal granule is at the in-process with the collision of heat transfer wall, the removal of the dirt layer such as calcium carbonate has been accelerated, further improve other types dirt layer and get rid of efficiency.
Meanwhile, the seed crystal circulation subsystem in the technical scheme can run simultaneously with the equipment, does not need to be stopped for processing, does not influence normal production, does not need to add other chemical components, and does not increase impurities. Compared with the traditional descaling method which needs one-time shutdown descaling within 10-15 days, the method reduces shutdown loss and improves production benefits; and after the descaling mode in the technical scheme is utilized for descaling, the descaling frequency is reduced to 6-8 months once, and the descaling cost is reduced.
The technical scheme is suitable for various devices, and the devices to be treated can be crystallizers, evaporators, heaters, heat exchangers and the like.
The crystal seeds are preferably gypsum crystal seeds, and the formed gypsum magnetic crystal seeds mainly remove stubborn calcium sulfate scales. For the removal of different scales, different kinds of crystal seeds can be selected, the crystal seeds need to select materials with the same components as the scale forming components, the crystal seeds magnetized under the action of a magnetic field induce the scale forming components with the same components to be attached to the crystal seeds, and the scale forming components are prevented from being attached to the wall surface of equipment to be treated to form a scale layer, so that the purposes of scale inhibition and scale removal are achieved. The scale inhibition and scale removal system for the magnetic crystal seeds of the gypsum in the technical scheme is also suitable for systems for inhibiting and removing scale after magnetization of other types of seed crystals, and is not limited to the application of the gypsum seed crystals or the removal of calcium sulfate scale.
The gypsum crystal seeds in the equipment to be treated can be added into the equipment to be treated through a feed inlet on the equipment to be treated, can also be added into a crystal seed circulation subsystem, and then are added into the equipment to be treated through the crystal seed circulation subsystem.
As shown in fig. 1, a crystallizer 8 is illustrated as a device to be treated.
Further, the seed crystal circulation subsystem further comprises a seed crystal container 1 and a seed crystal circulation pump 3, the seed crystal container 1 and the seed crystal circulation pump 3 are both connected to the seed crystal circulation loop, the equipment to be processed, the seed crystal circulation pump 3, the magnetic field generation device 2, the seed crystal container 1 and the equipment to be processed are connected to form a circulation loop, and all the equipment are connected sequentially through pipelines. The solution carrying the gypsum seed crystal in the equipment to be treated flows to the magnetic field generating device 2 under the action of the seed crystal circulating pump 3, flows into the seed crystal container 1, and is buffered in the seed crystal container 1 or flows back to the equipment to be treated through the seed crystal container 1.
The seed crystal container 1 can be also provided with an adding port, gypsum seed crystals are added into the seed crystal container 1 through the adding port, and the gypsum magnetic seed crystals in the seed crystal container 1 magnetize the newly added gypsum seed crystals and flow into the equipment to be treated together.
The seed crystal container 1 is internally provided with a stirrer for promoting the gypsum magnetic seed crystal slurry in the seed crystal circulation loop to be mixed with the newly added gypsum seed crystal, the stirrer is driven by a variable frequency motor to realize variable speed regulation, and the stirring speed is 0-20 r/min. The device to be treated is provided with a seed crystal circulating extraction outlet and a seed crystal slurry return port, the position of the seed crystal circulating extraction outlet is about 0.5m below the liquid level surface of the device to be treated, and the seed crystal slurry circulating return port is arranged above the liquid level surface and about 0.5m away from the liquid level surface. The seed crystal circulation subsystem is connected with the equipment to be treated through a seed crystal circulation extraction port and a seed crystal slurry return port to form a seed crystal circulation loop.
In some technical solutions, as shown in fig. 1 and 4, the magnetic crystal seed scale inhibiting and removing system for gypsum further includes a seed crystal slurry separation and extraction subsystem 4, and the magnetic crystal seed for gypsum in the equipment to be treated is subjected to solid-liquid separation and extraction through the seed crystal slurry separation and extraction subsystem 4, so as to be separated from components in the equipment to be treated and facilitate utilization of the crystal seed for gypsum. Fig. 4 illustrates a gypsum seed crystal as an example.
The seed crystal slurry separation and extraction subsystem 4 comprises a delayer 401, a seed crystal thickener 402, a settler 403, a first solid-liquid separator 404 and a first mother liquor buffer tank 405, the delayer 401 is connected with equipment to be treated, gypsum seed crystal slurry in the equipment to be treated enters the delayer 401, the gypsum seed crystal slurry is delaminated in the delayer 401 and is divided into gypsum seed crystal slurry and mother liquor, the gypsum seed crystal slurry is continuously separated and extracted, and the mother liquor flows back into the equipment to be treated.
The seed crystal slurry outlet of the delayer 401, the seed crystal thickener 402, the settler 403 and the first solid-liquid separator 404 are sequentially connected, gypsum seed crystal slurry in the delayer 401 sequentially flows into the seed crystal thickener 402, the settler 403 and the first solid-liquid separator 404 through the seed crystal slurry outlet for multiple separation, and gypsum seed crystals separated by the first solid-liquid separator 404 are collected and utilized. The mother liquor obtained by separation in each device flows back to the device to be treated, specifically, the mother liquor outlet of the delayer 401, the mother liquor outlet of the seed thickener 402, the mother liquor outlet of the settler 403 and the mother liquor outlet of the first solid-liquid separator 404 are all connected with the device to be treated and/or a first mother liquor buffer tank 405, and the first mother liquor buffer tank 405 is connected with the device to be treated. The separated mother liquor is buffered by the first mother liquor buffer tank 405 and then flows back to the equipment to be treated or directly flows back to the equipment to be treated, so that the mother liquor can be continuously utilized.
The equipment to be treated is connected with the delayer 401 through a connecting pipeline, and the height of one end of the connecting pipeline, which is connected with the delayer 401, is lower than that of one end of the connecting pipeline, which is connected with the equipment to be treated, so that the connecting pipeline extends obliquely, and the slurry can flow out smoothly. Wherein the inclination angle of the connecting pipeline is set to be 5-10 degrees.
Among them, the settler 403 is a tube settler.
The crystal seed slurry separation and extraction subsystem 4 recovers the gypsum crystal seeds from the mother liquor so as to recycle the gypsum crystal seeds, and meanwhile, the mother liquor flows back to the equipment to be treated for secondary treatment or utilization.
In some technical schemes, the magnetic field generating device 2 generates a strong alternating magnetic field, the magnetization of the fluid is enhanced by the high intensity magnetic field, the fluid flow is facilitated, and the problem of scaling caused by the accumulation of impurities in the fluid on the wall surface of the pipeline is further reduced. Preferably, the magnetic field intensity generated by the magnetic field generating device 2 is in the range of 5000-50000 gauss, and the high-intensity magnetic field fully magnetizes the gypsum crystal seeds, so that the scale inhibition and scale removal effects of the gypsum crystal seeds are improved.
Wherein, the high-intensity magnetic field with the magnetic field intensity range of 5000-50000 gauss is generated by an alternating power supply, the frequency of the alternating power supply is 2000Hz-20000Hz of medium/high frequency power supply, and the medium/high frequency power supply is converted into thousands to tens of thousands of Hz by common power frequency 50Hz alternating current.
Further, as shown in fig. 1 and 3, the magnetic field generating device 2 includes an inductive power supply 216, an electromagnetic coil 204, a magnetic field receiving assembly, a fluid delivery conduit 202, and a cooling circulation system. The induction power supply 216 is a medium/high frequency power supply with the frequency of 2000Hz-20000Hz, and the electromagnetic induction coil 204 is connected to the induction power supply 216, so as to generate the magnetic field intensity meeting the requirement of the equipment. The fluid delivery pipe 202 can be butted with a pipeline of the seed crystal circulation subsystem, and the butting mode can be various structural forms such as threaded connection, flange connection and the like.
The electromagnetic induction coil 204 is wound on the fluid conveying pipe 202, and a preset gap is left between the fluid conveying pipe 202 and the electromagnetic induction coil 204, so that short circuit caused by contact between the fluid conveying pipe 202 and the electromagnetic induction coil 204 is prevented, and matching of an electromagnetic induction system is realized.
The magnetic field receiving assembly is arranged in the fluid conveying pipeline 202 and comprises a magnetic gathering tube core 201 and a tube core supporting frame, specifically, the magnetic gathering tube core 201 is arranged in the fluid conveying pipeline 202, and the tube core supporting frame is used for fixing the magnetic gathering tube core 201 and the fluid conveying pipeline 202 to realize the magnetization effect on fluid media in the fluid conveying pipeline 202.
The magnetism gathering core 201 is a solid cylinder, the magnetism gathering core 201 is coaxial with the fluid conveying pipeline 202, namely, the magnetism gathering core 201 is installed in the center of the fluid conveying pipeline 202, and the purposes of attracting and uniformly distributing magnetic fields are achieved. The magnetism gathering tube core 201 is made of a cylindrical material, so that homogenization of a magnetic field is facilitated, and the solid material has a good absorption effect on the magnetic field.
Preferably, a pipe insulating layer 203 is arranged on the fluid conveying pipe 202, and the pipe insulating layer 203 is sandwiched between the electromagnetic induction coil 204 and the fluid conveying pipe 202, so that the pipe insulating layer plays a role in insulating the pipe and also plays a role in protecting the electromagnetic induction coil 204 by an isolation pad. Specifically, the preset gap between the fluid conveying pipe 202 and the electromagnetic induction coil 204 may be 2mm to 5mm, so as to avoid heat dissipation of the fluid conveying pipe 202.
The fluid conveying pipeline 202 is connected with a sealed heat-insulating cover 205, and the electromagnetic induction coil 204 is arranged between the pipeline heat-insulating layer 203 and the sealed heat-insulating cover 205, so that the electromagnetic induction coil 204 is protected, and the dispersion loss of a magnetic field is reduced.
Further, the electromagnetic induction coil 204 is a hollow spiral pipe, and the electromagnetic induction coil 204 is connected to the cooling circulation system. The cooling circulation system comprises a cooling circulation water tank 208 and a cooling water pump 207, wherein cooling fluid in the cooling circulation water tank 208 circularly flows in the electromagnetic induction coil 204 and the cooling circulation water tank 208 to exchange heat and reduce temperature, and the electromagnetic induction coil 204 is protected. The cooling water pump 207 is disposed at a cooling fluid outlet of the cooling circulation water tank 208, and the cooling water pump 207 provides a flow power for the cooling fluid to ensure the cooling fluid to flow circularly.
Further, a cooling pipeline is also arranged inside the induction power supply 216, and cooling fluid in the cooling circulation water tank 208 flows into the cooling pipeline to cool and protect the induction power supply 216. The cooling fluid circulates through the electromagnetic induction coil 204, the cooling pipe, and the cooling circulation water tank 208. Preferably, a heat exchange coil 210 is disposed in the cooling circulation water tank 208, and the heat exchange coil 210 exchanges heat with the cooling fluid in the cooling circulation water tank 208. Heat exchange coil 210 is provided as a metal coil, preferably stainless steel. A drain line 209 is also connected to the cooling circulation water tank 208.
Preferably, the electromagnetic induction coil 204 may be made of red copper, the turn moment and the turn moment distribution of the electromagnetic induction coil 204 are manufactured under actual conditions, the turn moment of the electromagnetic induction coil 204 is set to be equal to the turn moment or gradually increased from the inlet end to the outlet end, that is, the turn moment distribution may be sparse, the turn moment distribution may be dense, or the turn moment distribution may be dense and sparse, the hollow spiral tube with equal turn moment is convenient to process, and the processing cost is low. When the variable-turn moment is distributed, the turn moment is preferably gradually increased along the current inlet end to the current outlet end, so that the heat accumulation at the outlet end is reduced, and the magnetic field distribution and the heat transfer characteristics are met. The cross section of the electromagnetic induction coil 204 is a circular or rectangular hollow ring.
Furthermore, the magnetic field generating device 2 further includes a control cabinet 211, the control cabinet 211 is connected with a first pressure sensor 212, a first temperature sensor 213 and a first flow sensor 214, the first pressure sensor 212 measures the outlet pressure of the cooling circulation system, the first temperature sensor 213 measures the outlet temperature of the cooling circulation system, the first flow sensor 214 measures the outlet flow of the cooling circulation system, and monitors the temperature, the pressure and the flow of the cooling circulation system so as to adjust the flow state of the cooling circulation system.
The control cabinet 211 is also connected to a first level sensor 215 for detecting a change in the state of the liquid level in the cooling-cycle water tank 208, ensuring that the liquid level fluctuates within a certain range for timely replenishment and discharge. The control cabinet 211 is further connected with a second temperature sensor 217, and the second temperature sensor 217 measures the wall temperature of the fluid conveying pipe 202, so that the state of the fluid conveying pipe 202 and the temperature condition in the electromagnetic induction coil 204 can be known, problems can be found timely, and the flow rate of the cooling fluid can be adjusted.
The cooling circulation system is further provided with a first adjusting valve 206, the first adjusting valve 206 is connected to the circulation pipeline, the opening degree of the first adjusting valve 206 is adjustable to adjust the flow rate of the cooling fluid, the first adjusting valve 206 is connected to a control cabinet 211, and the control cabinet 211 can remotely adjust the first adjusting valve 206 as required.
Specifically, be equipped with PLC control system in the switch board 211, the last first regulating valve 206 of cooling circulation system and cooling water pump 207 all connect on PLC control system, and PLC control system embeds has PID control program, carries out real-time supervision and intelligent control to the technological parameter of each part in the device operation. The control cabinet 211 is connected to the inductive power supply 216 to control the current frequency of the inductive power supply 216. The control cabinet 211 realizes information acquisition of each sensor, and realizes linkage, feedback and protection functions according to the written control logic.
Among the above-mentioned technical scheme, magnetize the gypsum seed crystal in the seed crystal circulation circuit through magnetic field generating device 2 to realize automatic control to magnetic field generating device 2's operation, guarantee going on smoothly of gypsum seed crystal magnetization process, and then guarantee the scale inhibition scale removal effect.
The utility model provides an evaporation crystallization system, it is shown in combination figure 1-7, including crystallizer 8 and foretell seed crystal circulation subsystem, seed crystal circulation subsystem passes through the pipeline and is connected formation seed crystal circulation circuit with crystallizer 8, and the gypsum seed crystal in the seed crystal circulation subsystem is arranged in getting rid of the calcium sulfate dirt in crystallizer 8. The seed crystal circulation subsystem is arranged on the crystallizer 8 to perform scale inhibition and scale removal on the crystallizer 8, and the crystallization process and the scale inhibition and scale removal process are performed synchronously without stopping.
Compared with the existing chemical descaling, the scale inhibition and descaling method has the advantages of no need of stopping the machine, simplified process, reduced cost by 90 percent, and remarkable effect.
The technical scheme of the scale inhibition and scale removal system for the magnetic crystal seeds of gypsum can be directly applied to an evaporative crystallization system, namely equipment to be treated in the scale inhibition and scale removal system for the magnetic crystal seeds of gypsum is replaced by a crystallizer 8 in the technical scheme. The evaporative crystallization system is suitable for evaporative crystallization processes under various working conditions, is particularly suitable for chemical treatment processes with high calcium sulfate scale content such as sulfur-containing wastewater and industrial brine, and is beneficial to inducing inorganic salt in solution to crystallize and reducing impurities in crystallization.
Furthermore, the adding concentration of the gypsum seed crystal in the crystallizer 8 is set to be 20-25 g/L, and the discharging concentration of the gypsum seed crystal in the crystallizer 8 is set to be 30-40g/L, so that the normal operation of the crystallization process is maintained. Gypsum seeds in crystallizer 8 are added through seed vessel 1 of the crystallization circulation subsystem.
In some embodiments, as shown in fig. 2 and 4, the seed slurry separation and withdrawal subsystem 4 is connected to the crystallizer 8, the delayer 401 is connected to the crystallizer 8 so that the slurry containing gypsum seeds enters the delayer 401, the slurry containing gypsum seeds is separated in the delayer 401 to form gypsum seed slurry and mother liquor (generally, the gypsum seed slurry rises to the upper layer of the delayer 401, and the mother liquor sinks to the lower layer of the delayer 401), and the mother liquor outlet of the delayer 401 is connected to the crystallizer 8 and/or the first mother liquor buffer tank 405 so that the mother liquor flows back to the crystallizer 8; the gypsum seed slurry is connected to the seed thickener 402 through the slurry outlet of the delayer 401, separation is carried out again, the gypsum seed slurry obtained through separation enters the settler 403 through the slurry outlet of the seed thickener 402, and the mother liquor obtained through separation flows into the crystallizer 8 and/or the first mother liquor buffer tank 405 through the mother liquor outlet of the seed thickener 402; in the same way, the gypsum seed crystal slurry is separated again in the solid-liquid separator.
Further, the crystallizer 8 is connected with the delayer 401 through a connecting pipeline, and the height of one end of the connecting pipeline, which is connected with the delayer 401, is lower than that of one end of the connecting pipeline, which is connected with the crystallizer 8, so that the connecting pipeline extends obliquely, and slurry can flow out smoothly. Wherein the inclination angle of the connecting pipeline is set to be 5-10 degrees.
And separating the slurry containing the gypsum crystal seeds in the crystallizer 8 for multiple times to obtain the gypsum crystal seeds and mother liquor, reusing the gypsum crystal seeds, and refluxing the mother liquor into the crystallizer 8 for treatment.
The first mother liquor buffer tank 405 may be connected directly to the crystallizer 8 and may also be connected to the heater 9. The crystallizer 8 is connected with the heater 9, the heater 9 circularly heats the mother liquor in the crystallizer 8, the first mother liquor buffer tank 405 is connected to the heater 9 and can be heated by the heater 9 and then flows back to the crystallizer 8, so that the temperature balance in the crystallizer 8 is kept, and the crystallization efficiency is ensured.
When the gypsum seed crystal is adopted, the seed crystal slurry separation and extraction subsystem 4 recovers the gypsum seed crystal, and the mother liquor containing the salt slurry flows back to the crystallizer 8 to continue crystallization, so that the continuous and efficient process of the salt slurry crystallization process is ensured.
Preferably, a back flushing opening is arranged at the lower cone outlet of the crystal seed thickener 402, the feed is used as the back flushing liquid, the gypsum crystal seed slurry is back flushed and cleaned, the axial flow rate of the back flushing liquid is controlled to be 5-10m/s, and the salinity in the desalted gypsum crystal seed is controlled to be within 1%.
That is, when the seed crystal is selected from other components, the salt content in the desalted seed crystal is controlled to be within 1%.
The settler 403 is an inclined tube settler 403, the inclined tube settler 403 is preferably in a honeycomb inclined tube type, the length of an inclined tube is 1m, the inclination angle is 60 degrees, the diameter of an inscribed circle is 35-50mm, and the material is glass fiber reinforced plastic or polyvinyl chloride.
The first solid-liquid separator 404 preferably employs a horizontal spiral discharge decanter centrifuge, with a preferred range of filterable solid particle diameters of 0.01-3mm and a preferred range of centrifuge separation factors of 2000-. The first solid-liquid separator 404 may also be a filter press, which is a box filter press, for dehydrating the gypsum seed crystals.
The first mother liquor buffer tank 405 is provided with a heat-insulating layer, so that the temperature of the mother liquor is prevented from suddenly dropping to cause the mother liquor to precipitate salt and block pipelines, and the thickness of the heat-insulating layer is preferably 50-100 mm. The first mother liquor buffer tank 405 is provided with a stirrer, preferably a gate type stirring paddle, and the stirring speed is controlled to be 10-40 r/min. And the mother liquor inlet position of the first mother liquor buffer tank 405 is lower than the mother liquor outlet positions of the seed thickener 402, the settler 403 and the first solid-liquid centrifuge.
In some embodiments, as shown in fig. 2 and 5, a salt slurry separation and extraction subsystem 6 is further connected to the crystallizer 8 to separate the salt slurry to obtain a solid salt product. The salt slurry separation and extraction subsystem 6 comprises a salt slurry thickener 601, a second solid-liquid separator 602 and a second mother liquor buffer tank 603, the salt slurry thickener 601 is connected with the crystallizer 8, salt slurry in the crystallizer 8 enters the salt slurry thickener 601 for solid-liquid separation to obtain high-concentration salt slurry and mother liquor through separation, the high-concentration salt slurry enters the second solid-liquid separator 602 through a salt slurry outlet of the salt slurry thickener 601 for solid-liquid separation again, and solid salt and mother liquor are obtained through separation. The slurry outlet of the salt slurry thickener 601 and the slurry outlet of the second solid-liquid separator 602 are connected with the second mother liquid buffer tank 603 and/or the crystallizer 8, the second mother liquid buffer tank 603 is connected with the crystallizer 8, and the mother liquid directly flows back to the crystallizer 8 or flows back to the crystallizer 8 after being buffered by the second mother liquid buffer tank 603.
The second mother liquor buffer tank 603 may be directly connected to the crystallizer 8 or connected to the heater 9, and the mother liquor is heated by the heater 9 and then refluxed to the crystallizer 8.
Specifically, a back flushing opening is formed in the lower cone outlet of the salt slurry thickener 601, feeding is used as back flushing liquid, back flushing cleaning is carried out on the salt slurry, the axial flow rate of the back flushing liquid is controlled to be 5-10m/s, and the salt slurry solid-liquid ratio at the outlet of the salt slurry thickener 601 is controlled to be 50-70%.
The second solid-liquid separator 602 preferably adopts a horizontal two-stage pusher centrifuge, the preferred range of the diameter of the filterable solid particles is more than 0.15mm, the preferred range of the separation factor of the horizontal two-stage pusher centrifuge is 200-1200, and the water content of the separated salt slurry material is controlled within 5%.
The second mother liquor buffer tank 603 is also provided with a stirrer, preferably a gate type stirring paddle, and the stirring speed is controlled to be 10-40 r/min. The second mother liquor buffer tank 603 is also provided with a heat insulation layer to prevent the temperature of the mother liquor from suddenly dropping to cause the mother liquor to precipitate salt and block pipelines, and the thickness of the heat insulation layer is preferably 50-100 mm. The mother liquor inlet position of the second mother liquor buffer tank 603 should be lower than the mother liquor outlet positions of the salt slurry thickener 601 and the second solid-liquid centrifuge.
When the discharge amount of the salt slurry of the crystallizer 8 is less than 200kg/h, a four-foot large-flip type centrifuge is preferably adopted.
In some technical solutions, as shown in fig. 2 and fig. 6, the evaporative crystallization system further includes a heater 9 and a vapor compression subsystem 7, a vapor outlet of the crystallizer 8 is connected to the vapor compression subsystem 7, a heat source outlet of the vapor compression subsystem 7 is connected to a heat source side inlet of the heater 9, and a cold source side of the heater 9 is connected to the crystallizer 8 to form a crystallization circulation loop. The mother liquid in the crystallizer 8 flows into the cold source side of the heater 9 to exchange heat with the heat source side of the heater 9 and then flows back into the crystallizer 8, the heat on the heat source side of the heater 9 comes from the vapor compression subsystem 7, the vapor compression subsystem 7 heats the vapor flowing out of the crystallizer 8 and then serves as a heat source for heating the mother liquid, and the heat of the vapor flowing out of the crystallizer 8 is fully utilized. A heat source side inlet of the heater 9 is connected with the steam compression subsystem 7, a heat source side outlet of the heater 9 is connected with the condensed water tank 10, and hot steam forms condensed water after heat exchange in the heater 9 and is discharged into the condensed water tank 10.
The cold source sides of the crystallizer 8 and the heater 9 are connected through a pipeline, the pipeline is connected with an evaporation circulating pump 5, mother liquor materials in the crystallizer 8 are input to the heater 9 under the driving of the evaporation circulating pump 5, the mother liquor materials complete heat exchange in the heater 9 and then return to the crystallizer 8 to complete flash evaporation, and concentrated crystallization is achieved to obtain solid crystalline salt.
A sampling port is arranged at the cold source side inlet and outlet of the heater 9 and used for detecting the concentration of gypsum crystal seeds in the circulating liquid, and after the specified concentration is reached, the crystallizer 8 can discharge the gypsum crystal seed slurry through the crystal seed slurry separation and extraction subsystem 4.
The medium flow rate of the evaporation circulating liquid in the heat exchange pipe of the heater 9 is controlled to be 1.0-2.5m/s, and the solid-liquid ratio of the evaporation circulating liquid is controlled to be 20-30%; when the medium is a chloride ion inorganic salt solution, the heat exchange tube of the heater 9 is preferably TA2 material.
The steam compression subsystem 7 comprises a compressor 701, a gas-liquid separator 702, a water tank 705, an oil supply pump 712, an oil tank 703, a liquid loop and an oil loop, steam flowing out of a secondary steam outlet of the crystallizer 8 enters the compressor 701, enters the gas-liquid separator 702 after being compressed in the compressor 701, secondary steam obtained by separation of the gas-liquid separator 702 enters a heater 9 as a heat exchange heat source, liquid obtained by separation of the gas-liquid separator 702 flows into the water tank 705, flows into the compressor 701 through the liquid loop connected to the water tank 705, and is compressed again. An oil circuit, an oil feed pump 712, and an oil tank 703 are connected to the compressor 701, and the pressure oil in the compressor 701 flows into the oil tank 703 and the oil feed pump 712 through the oil circuit, and the oil feed pump 712 pressurizes the pressure oil and then flows into the compressor 701.
Wherein, the compressor 701 is also connected with a vapor filter 704, vapor flowing out from the secondary vapor outlet of the crystallizer 8 is filtered by the vapor filter 704 and then enters the compressor 701, and the service life of the compressor 701 is prolonged. A water supply pump 706 and a water supply filter 707 are also connected to the liquid circuit between the water tank 705 and the compressor 701. An oil supply filter 713 is also connected between the oil supply pump 712 and the compressor 701. Wherein, the water supply filter 707 and the oil supply filter 713 can both adopt Y-shaped filters, and the filtering precision is 80 meshes.
A second level sensor 708 is attached to the water tank 705, a second regulating valve 709 is attached to a water supply pipe communicating with the water tank 705, and the opening degree of the second regulating valve 709 is regulated according to the liquid level state of the second level sensor 708, thereby ensuring the liquid level of the water tank 705 to be stable. The water temperature in the water tank 705 returning to the compressor 701 is not lower than the inlet steam temperature of the compressor 701.
Wherein the outlet pressure of the oil supply pump 712 is preferably 4bar to 10 bar. The oil temperature in the oil tank 703 should not be higher than 60 ℃. The oil tank 703 is provided with a cooling coil pipe, a cooling medium is input into the cooling coil pipe to cool the cooling oil in the oil tank 703, and the cooling coil pipe can adopt an inner-outer double-coil pipe type. The oil tank 703 adopts cooling water as a cooling medium, a third regulating valve 710 and a third temperature sensor 711 are installed on a water inlet pipe of the oil tank 703, and the opening degree of the third regulating valve 710 is controlled according to the temperature collected by the third temperature sensor 711, so that the temperature of the cooling oil is ensured to be in a reasonable range.
Preferably, when the steam flow of the compressor 701 is less than 100m3At/min, a single-screw compressor is adopted; when the steam flow is between 50m3/min～500m3At/min, Roots-type compressor is used, when the steam flow is higher than 200m3At/min, a centrifugal compressor is used.
Referring to fig. 2 and 7, the crystallizer 8 is set in an axial reverse circulation mode, the crystallizer 8 includes an evaporation section 804, a crystallization section 806, and a salt leg section 807, a circulation liquid outlet pipe 803 and a demister 802 are provided in the crystallizer 8, the circulation liquid outlet pipe 803 extends into the evaporation section 804, and the demister 802 is provided in the evaporation section 804 and is located in the gas phase space above the circulation liquid outlet pipe 803.
One end of the circulating liquid outlet pipe 803 extending into the evaporation section 804 is in a bell mouth shape, the evaporation section 804 is in a cylindrical barrel shape, and the top of the evaporation section 804 is provided with an upper cone 801; the crystallization section 806 is conical, the circulating liquid outlet pipe 803 extends out of the crystallizer 8 along the crystallization section 806, and the crystallization section 806 is provided with a circulating liquid inlet 805 so that the mother liquid separated in the seed crystal circulation subsystem can return to the crystallizer 8; the salt leg section 807 is of a cylinder structure, the sectional area of the salt leg section is 10-15% of that of the evaporation section, a back flushing opening 808 is formed in the salt leg section 807, and materials flow into the crystallizer 8 through the back flushing opening 808 to prevent salt crystals from being blocked in the salt leg section 807.
The height of the vapor phase space of the crystallizer 8 is set to be more than 2m, the distance from one end of the circulating liquid outlet pipe 803 extending into the evaporation section to the liquid level in the evaporation section is set to be 0.5-1.0m, and the evaporation intensity of the crystallizer 8 is controlled to be 1.0-1.5m3/m3. Among them, the demister 802 is preferably a wire mesh demister.
The crystallization section 806 is provided with a seed crystal sampling port so as to detect the concentration of gypsum seed crystals in the circulating liquid, and high-concentration gypsum seed crystal slurry is discharged after the specified concentration is reached. The salt leg section 807 is provided with a salt concentration sampling port so as to detect the concentration of the salt slurry, and after the specified concentration is reached, the high-concentration salt slurry can be discharged.
The barrel of evaporation zone 804 should set up the reinforcement circle, and the reinforcement circle sets up 1 every 1m along barrel axial direction, improves barrel intensity.
In the above scheme, the heater 9 and the crystallizer 8 should be further heat-insulated, and preferably heat-insulated rock wool or heat-insulated material capable of resisting temperature above 200 ℃ is adopted.
The technical scheme can be applied to the evaporation process of zero discharge of high-salinity wastewater and the evaporation crystallization operation unit in the salt manufacturing industry. The device is particularly suitable for the desulfurization wastewater zero-discharge evaporation process, the pesticide wastewater zero-discharge evaporation process, other high-salt-content wastewater evaporation treatment processes and a salt production evaporation system. The technical scheme has the advantages of good scale inhibition and scale removal effect, wide application range, convenience in operation, low operation cost and the like, and in view of the fact that high-salinity wastewater generated in the industries of chemical engineering, pharmacy and the like mainly contains calcium carbonate and calcium sulfate scale, the gypsum magnetic crystal seed scale inhibition and removal can be suitable for the water quality of most of high-salinity wastewater, the calcium sulfate scale and the calcium carbonate scale are effectively inhibited and removed in a high-salinity wastewater zero-discharge evaporation system, the gypsum magnetic crystal seed scale inhibition and removal method is particularly applied to a power plant desulfurization wastewater zero-discharge evaporation process, the cost of a hardness removal pretreatment agent in the early stage of zero discharge is greatly reduced, the scale inhibition and removal cost is.
In the description of the present invention, it should be noted that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, and are only for convenience of description and simplification of the description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood as appropriate by those of ordinary skill in the art.
In the description of the present invention, the terms "plurality", and "plural" mean two or more unless otherwise specified.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The gypsum magnetic crystal seed scale inhibition and removal system is characterized by comprising a seed crystal circulation subsystem, wherein the seed crystal circulation subsystem is connected with equipment to be treated through a pipeline to form a seed crystal circulation loop, the seed crystal circulation subsystem comprises a magnetic field generating device, and the magnetic field generating device is used for magnetizing gypsum seed crystals flowing through the magnetic field generating device to form gypsum magnetic seed crystals.
2. The gypsum magnetic crystal seed scale inhibition and removal system according to claim 1, wherein the seed crystal circulation subsystem further comprises a seed crystal container and a seed crystal circulation pump, both of which are connected to the seed crystal circulation loop.
3. The gypsum magnetocrystalline scale inhibition and removal system according to claim 1, wherein the magnetic field generating device generates a strong alternating magnetic field, and the magnetic field intensity generated by the magnetic field generating device ranges from 5000-50000 gauss.
4. The gypsum magnetic crystal scale inhibiting and removing system according to claim 1, wherein the magnetic field generating device comprises an induction power supply, an electromagnetic induction coil, a magnetic field receiving assembly, a fluid conveying pipeline and a cooling circulation system, wherein the induction power supply supplies alternating current to the electromagnetic induction coil, the electromagnetic induction coil is wound on the fluid conveying pipeline, the magnetic field receiving assembly is arranged in the fluid conveying pipeline, the fluid conveying pipeline is connected with a pipeline of the crystal seed circulation loop, the electromagnetic induction coil is a hollow spiral pipe, and the electromagnetic induction coil is connected with the cooling circulation system.
5. The scale inhibiting and removing system of the magnetic crystal seed of gypsum as claimed in any one of claims 1 to 4, it is characterized by also comprising a seed crystal slurry separation and extraction subsystem which is connected with the equipment to be treated, the seed crystal slurry separation and extraction subsystem comprises a delayer, a seed crystal thickener, a settler, a first solid-liquid separator and a first mother liquor buffer tank, the delayer is connected with the equipment to be treated, a seed crystal slurry outlet of the delayer, the seed crystal thickener, the settler and the first solid-liquid separator are sequentially connected, the mother liquor outlet of the delayer, the mother liquor outlet of the seed thickener, the mother liquor outlet of the settler and the mother liquor outlet of the first solid-liquid separator are all connected with the equipment to be treated and/or the first mother liquor buffer tank, and the first mother liquor buffer tank is connected with the equipment to be treated.
6. An evaporative crystallization system comprising a crystallizer, characterized by comprising a seed circulation subsystem according to any one of claims 1 to 5 connected to the crystallizer by a line to form a seed circulation loop.
7. The evaporative crystallization system of claim 6, wherein the crystallizer is further connected with a salt slurry separation and extraction subsystem, the salt slurry separation and extraction subsystem comprises a salt slurry thickener, a second solid-liquid separator and a second mother liquor buffer tank, the salt slurry thickener is connected with the crystallizer, a salt slurry outlet of the salt slurry thickener is connected with the second solid-liquid separator, a slurry outlet of the salt slurry thickener and a slurry outlet of the second solid-liquid separator are connected with the second mother liquor buffer tank and/or the crystallizer, and the second mother liquor buffer tank is connected with the crystallizer.
8. The evaporative crystallization system of claim 6, further comprising a heater and a vapor compression subsystem, wherein the vapor outlet of the crystallizer is connected to the vapor compression subsystem, the heat source outlet of the vapor compression subsystem is connected to the heat source side inlet of the heater, and the cold source side of the heater is connected to the crystallizer to form a crystallization circulation loop.
9. The evaporative crystallization system of claim 8, wherein the vapor compression subsystem comprises a compressor, a gas-liquid separator, a water tank, a feed pump, a fuel tank,
a steam outlet of the crystallizer is connected with an inlet of the compressor, a steam outlet of the compressor is connected with the gas-liquid separator, a steam outlet of the gas-liquid separator is connected with the heater, a liquid outlet of the gas-liquid separator is connected with the water tank, and the water tank is connected with an inlet of the compressor;
the oil outlet of the compressor is connected with the oil tank, and the oil tank and the oil inlet of the compressor are connected with the oil supply pump.
10. The evaporative crystallization system of claim 6, wherein the crystallizer is set in an axial reverse circulation type, the crystallizer comprises an evaporation section, a crystallization section and a salt leg section, a circulating liquid outlet pipe and a demister are arranged in the crystallizer, the circulating liquid outlet pipe extends into the evaporation section, the demister is arranged in the evaporation section and is positioned above the circulating liquid outlet pipe, the crystallization section is provided with a seed crystal sampling port, and the salt leg section is provided with a salt concentration sampling port and a reverse flushing port.
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| CN110171859A (en) * | 2019-06-20 | 2019-08-27 | 中国科学院理化技术研究所 | Gypsum magnetocrystalline kind anti-scale descaling system and evaporation and crystallization system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110171859A (en) * | 2019-06-20 | 2019-08-27 | 中国科学院理化技术研究所 | Gypsum magnetocrystalline kind anti-scale descaling system and evaporation and crystallization system |
| CN110171859B (en) * | 2019-06-20 | 2021-07-20 | 中国科学院理化技术研究所 | Scale inhibition and scale removal system for gypsum magnetic crystal seeds and evaporative crystallization system |
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