CN117985800A - Evaporation crystallization equipment for treating high-salt wastewater - Google Patents
Evaporation crystallization equipment for treating high-salt wastewater Download PDFInfo
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- CN117985800A CN117985800A CN202410397330.2A CN202410397330A CN117985800A CN 117985800 A CN117985800 A CN 117985800A CN 202410397330 A CN202410397330 A CN 202410397330A CN 117985800 A CN117985800 A CN 117985800A
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- 238000001704 evaporation Methods 0.000 title claims abstract description 79
- 230000008020 evaporation Effects 0.000 title claims abstract description 69
- 238000002425 crystallisation Methods 0.000 title claims abstract description 32
- 239000002351 wastewater Substances 0.000 title claims abstract description 27
- 230000008025 crystallization Effects 0.000 title claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 104
- 238000000926 separation method Methods 0.000 claims abstract description 71
- 238000010438 heat treatment Methods 0.000 claims abstract description 3
- 239000007791 liquid phase Substances 0.000 claims abstract description 3
- 239000012071 phase Substances 0.000 claims abstract description 3
- 150000003839 salts Chemical class 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 230000000630 rising effect Effects 0.000 claims description 7
- 230000000694 effects Effects 0.000 abstract description 13
- 238000004065 wastewater treatment Methods 0.000 abstract description 4
- 239000013078 crystal Substances 0.000 description 9
- 238000009835 boiling Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000013505 freshwater Substances 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000006911 nucleation Effects 0.000 description 1
- 238000010899 nucleation Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The application relates to an evaporation crystallization device for treating high-salt wastewater, which belongs to the technical field of wastewater treatment, and comprises a heater for heating feed liquid and an evaporation crystallizer connected with the heater, wherein a gas-liquid separation device for separating gas phase from liquid phase is arranged on the evaporation crystallizer, the gas-liquid separation device is arranged on the outer wall of the evaporation crystallizer in a sliding manner, and the sliding direction slides along the vertical direction; the outer wall of the evaporation crystallizer is provided with a positioning component, the positioning component comprises a slide rail and a support frame, the slide rail is fixed on the outer wall of the evaporation crystallizer along the vertical direction, the support frame is arranged on the slide rail in a sliding manner and slides along the vertical direction, and the position, away from the slide rail, of the support frame is detachably connected with the gas-liquid separation device; the application has the effect of ensuring that the evaporation crystallization equipment and the heater can conveniently move in the pilot test stage and the overall height is reduced.
Description
Technical Field
The application relates to the technical field of wastewater treatment, in particular to an evaporation crystallization device for treating high-salt wastewater.
Background
At present, in the evaporation treatment process of high-salt wastewater, the boiling point of the high-salt wastewater is increased along with the increase of the salt concentration, so that the salt concentration in the wastewater reaches the crystallization requirement, and the water can be evaporated only by gradually increasing the temperature to be reached, so that the salt in the wastewater is crystallized and separated out. High salt wastewater refers to wastewater containing organic matter and at least a mass fraction of Total Dissolved Solids (TDS) greater than 3.5%.
The vertical height of the existing evaporator and crystallizer equipment is more than 10 meters, so that the temperature requirement is met.
However, many treatment processes often require a pilot stage of experimentation, which is a larger scale trial performed after laboratory studies and small scale trials. The method is a test stage before the formal delivery of the product, can help to verify and optimize the production process, equipment, operation flow and the like, reduces the equipment in the pilot test stage in an equal ratio, and often cannot be tested, and has the complete effect of the implementation stage. In addition, the pilot plant is convenient to move and needs to be transported by a container, so that the heights of the evaporator and the crystallizer are less than 4.2 meters, and the problem needs to be solved.
Disclosure of Invention
In order to ensure that the evaporation and crystallization equipment and the heater in the pilot plant stage can be conveniently moved and the overall height is reduced, the application provides the evaporation and crystallization equipment for treating the high-salt wastewater.
The application provides evaporation crystallization equipment for treating high-salt wastewater, which adopts the following technical scheme:
The evaporation crystallization equipment for treating the high-salt wastewater comprises a heater for heating feed liquid and an evaporation crystallizer connected with the heater, wherein a gas-liquid separation device for separating gas phase from liquid phase is arranged on the evaporation crystallizer, and the gas-liquid separation device is arranged on the outer wall of the evaporation crystallizer in a sliding manner, and the sliding direction slides along the vertical direction; the outer wall of the evaporation crystallizer is provided with a positioning component, the positioning component comprises a slide rail and a support frame, the slide rail is fixed on the outer wall of the evaporation crystallizer along the vertical direction, the support frame is arranged on the slide rail in a sliding manner and slides along the vertical direction, and the position, away from the slide rail, of the support frame is detachably connected with the gas-liquid separation device; the support frame is provided with a driving component for driving the support frame to move on the sliding rail.
By adopting the technical scheme, the heater heats the feed liquid by utilizing fresh steam or steam at the outlet of the compressor, the feed liquid is sent into the evaporation crystallizer for evaporation crystallization, and gas-liquid separation is carried out by the gas-liquid separation device, the heater is arranged beside the evaporation crystallizer and the height difference of the two is met, so that the feed liquid in the heater is prevented from boiling, the gas-liquid separation device is independently arranged on the evaporation crystallizer, on one hand, the height of the whole equipment can be reduced, and on the other hand, the gas-liquid separation device can be flexibly replaced, so that different sizes are adopted, and the effect of gas-liquid capability is ensured; the driving assembly provides power for the positioning assembly, and the positioning assembly drives the gas-liquid separation device to displace relative to the evaporation crystallizer, so that the vertical height of the gas-liquid separator is changed, and the height requirement of gas-liquid separation is met.
Optionally, the water treatment amount of the evaporation crystallizer is 0.5m3/h, the TDS of the inlet water is 160000mg/L, the diameter of the evaporation crystallizer is 1000mm, and the rising speed in the evaporation crystallizer during gas-liquid separation is far lower than 1m/s.
By adopting the technical scheme, the lower the rising gas speed during gas-liquid separation in the evaporation crystallizer is, the smaller the entrainment quantity is, so that the effect of shortening the height of the evaporation crystallizer can be achieved when the same gas-liquid separation effect is achieved; the diameter of the evaporating crystallizer is larger than that of the evaporating crystallizer selected by the conventional evaporating water amount, so that the enough crystal slurry residence time can be ensured, the granularity of the crystallized salt is ensured, and the purity of the crystallized salt product is improved.
Optionally, the drive assembly includes gear, rack and first motor, the rack is fixed on the slide rail, and rack length direction sets up along vertical direction, gear rotation sets up on the support frame, and the relative support frame rotation of gear, first motor is fixed on the support frame, and the output and the gear fixed connection of first motor, gear and rack engagement.
Through adopting above-mentioned technical scheme, first motor drive gear rotates, thereby gear and rack meshing make the support frame produce the displacement relative slide rail to change the vertical position of support frame.
Optionally, a second motor and a hydraulic cylinder fixedly connected with the rotating end of the second motor are slidably arranged on the gear, the second motor is arranged along the direction close to or far away from the sliding rail, and the second motor is positioned at one side of the gear away from the first motor; the output shaft of the second motor is perpendicular to the piston shaft of the hydraulic cylinder, the support frame comprises a telescopic rod and a positioning rod, the positioning rod is in sliding connection with the sliding rail, and the telescopic rod is used for connecting the positioning rod and the gas-liquid separation device.
Through adopting above-mentioned technical scheme, start the second motor, the second motor can change the position of pneumatic cylinder, makes pneumatic cylinder one end towards the evaporation crystallizer other end towards gas-liquid separation equipment, starts the pneumatic cylinder, and the pneumatic cylinder can remove gas-liquid separation equipment to the direction of keeping away from evaporation crystallizer to change the relative position between them, be convenient for satisfy the position demand of gas-liquid separation. The second machine that slides and set up can drive the pneumatic cylinder and take place the displacement, makes the pneumatic cylinder not collide with rack and slide rail when gear rotation, has guaranteed the normal use of gear.
Optionally, a sliding groove is formed in the side wall of the gear, the sliding groove is formed in the length direction of any diameter of the gear, a sliding block is fixed on the second motor and slides in the sliding groove, a spring is arranged on the gear, and the spring is fixed between the sliding block and the groove wall of the end portion of the sliding groove.
By adopting the technical scheme, after the hydraulic cylinder is started, the spring is passively deformed, at the moment, one end of the hydraulic cylinder is abutted with the gas-liquid separation device, and the other end of the hydraulic cylinder is abutted with the outer wall of the evaporation crystallizer; when the hydraulic cylinder is used, the piston end of the hydraulic cylinder is recovered, and at the moment, the spring is required to recover deformation, the sliding block is driven to slide in the sliding groove, and finally the hydraulic cylinder is driven to move, so that the hydraulic cylinder is ensured not to collide with the rack and the sliding rail.
Optionally, be fixed with the push pedal on the piston end of pneumatic cylinder and with push pedal fixed connection's rubber pad, the rubber pad is located the push pedal and deviates from the lateral wall of pneumatic cylinder.
Through adopting above-mentioned technical scheme, the area of contact between pneumatic cylinder piston end and the gas-liquid separation device has been increased in the setting of push pedal, and the setting of rubber pad has avoided the rigidity collision between push pedal and the gas-liquid separation device.
Optionally, the telescopic link is provided with two and corresponds the both ends that distribute at the locating lever, locating lever and two all be provided with the diagonal brace between the telescopic link, diagonal brace one end and locating lever fixed connection, the other end and corresponding telescopic link sliding connection.
Through adopting above-mentioned technical scheme, the existence of diagonal brace has strengthened the bearing capacity of support frame, and diagonal brace cooperation locating lever and telescopic link have formed stable triangle-shaped structure, and diagonal brace tip and telescopic link sliding connection's mode makes the telescopic link move the time and does not take place to hinder with the diagonal brace simultaneously.
Optionally, the telescopic link is kept away from the tip threaded connection of locating lever and is had the staple bolt, and the staple bolt is used for fixed gas-liquid separation device.
Through adopting above-mentioned technical scheme, adopt the substitution of the not unidimensional staple bolt of connected mode of screw thread can be quick to satisfy the fixed gas-liquid separation device's of different diameters demand of centre gripping.
Optionally, the staple bolt still is used for fixed heater, and the slide rail is fixed subaerial this moment, and the support frame is located between slide rail and the heater, and the telescopic link is used for connecting locating lever and staple bolt.
Through adopting above-mentioned technical scheme, in order to guarantee that the interior feed liquid of heater does not boil, avoid taking place the phenomenon of heat exchange tube dry pipe, need regulate and control the difference in height between evaporation crystallizer and the heater, fix the slide rail subaerial, support the heater fixedly through the support frame, the staple bolt is fixed this moment is the heater, change the vertical height of heater through drive assembly and positioning subassembly to change the difference in height between heater and the evaporation crystallizer, make support frame, drive arrangement, adjusting device all realize two kinds of application environment.
Optionally, the support frame is fixed with the flank board, is provided with the bolt that is used for both fixed between flank board and the slide rail.
Through adopting above-mentioned technical scheme, after the support frame slides the assigned position, thereby accomplish the fixed of support frame and slide rail through the bolt with flank board and slide rail is fixed, alleviateed the support frame and adjusted the atress between assigned position back, gear and the rack.
In summary, the present application includes at least one of the following beneficial technical effects:
the heater heats the feed liquid by using fresh steam or outlet steam of the compressor, the size of the heater depends on the area of the heater (the larger the area is, the number of heat exchange tubes with the same heat exchange tube length is large, and thus the diameter is large), the area of the heater is related to the effective heat transfer temperature difference (the effective heat transfer temperature difference is related to the temperature of the fresh steam or outlet steam of the compressor, the temperature of secondary steam and the boiling point of the feed liquid) and the heat exchange coefficient (the heat exchange coefficient is generally an empirical value), the temperature rise of the feed liquid can be within a proper range (1-2 ℃) only if the area of the heater is proper, and then proper supersaturation degree is provided for crystallization of the feed liquid (only supersaturation can be crystallized, and the supersaturation degree cannot be too large and burst nucleation can be generated, fine crystals are generated), and in addition, the area of the heater is proper to ensure enough evaporation amount; the larger the diameter of the evaporative crystallizer is under the condition that the treatment capacity is the same, on one hand, the lower the rising gas speed of gas is during gas-liquid separation, the less entrainment is carried out, so that the quality of fresh water is improved; on the other hand, the larger the diameter is, the longer the residence time is, so that the grain diameter of the crystal is increased, and the quality of the crystal salt is improved. However, the evaporating crystallizer is not suitable for being too large in diameter, the occupied area is increased, the equipment cost is increased, and the equipment load is increased due to the too large diameter;
The heater utilizes live steam or compressor export steam to heat the feed liquid, provides suitable supersaturation degree for the crystallization of feed liquid, and the evaporation crystallizer sets up gas-liquid separation device alone and can reduce equipment height on the one hand, and on the other hand can nimble adjustment gas-liquid separation device's size, guarantees gas-liquid separation effect, and the higher the gas-liquid separation device's height promptly, the better the effect of gas-liquid separation. The sliding component can change the position of the gas-liquid separation device relative to the evaporation crystallizer, so that the wastewater treatment requirement is further met;
The water treatment amount of the evaporation crystallizer is 0.5m3/h, the TDS of the inlet water is 160000mg/L, the diameter of the evaporation crystallizer is 1000mm, the rising speed in the evaporation crystallizer during gas-liquid separation is far lower than 1m/s, the lower the gas speed is, the less the entrainment amount is, so that the height of the evaporation crystallizer can be shortened when the same gas-liquid separation effect is achieved; the diameter of the evaporating crystallizer is larger than that of the evaporating crystallizer selected by the conventional evaporating water amount, so that enough crystal slurry residence time can be ensured, and the granularity of crystallized salt is ensured, thereby improving the purity of crystallized salt products
The support frame, the positioning assembly and the driving assembly can be used between the ground and the heater, and can also be used between the evaporation crystallizer and the gas-liquid separation device, so that two application scenes are met, when the support frame, the positioning assembly and the driving assembly are applied between the ground and the heater, the heater can move in a direction far away from or near to the evaporation crystallizer through the support frame, the positioning assembly and the driving assembly, and meanwhile, the height difference between the heater and the evaporation crystallizer can be changed; when the device is applied between the evaporation crystallizer and the gas-liquid separation device, the position of the gas-liquid separation device relative to the evaporation crystallizer in the vertical direction can be adjusted, and the gas-liquid separation device can be pushed in the direction away from the evaporation crystallizer;
The screw connection mode is adopted to quickly replace hoops with different sizes, so that the requirements of clamping and fixing gas-liquid separation devices with different diameters and heaters are met;
The existence of diagonal brace has strengthened the bearing capacity of support frame, and diagonal brace cooperation locating lever and telescopic link have formed stable triangle-shaped structure, and diagonal brace tip and telescopic link sliding connection's mode makes the telescopic link not take place the hindrance with the diagonal brace when moving simultaneously.
Drawings
FIG. 1 is a schematic diagram of an embodiment of the present application applied to an evaporative crystallizer;
FIG. 2 is a schematic diagram of a heater according to an embodiment of the present application;
FIG. 3 is a schematic view of the configuration of the location of the protruding drive assembly;
Fig. 4 is a schematic view of a partial structure of the position of the protruding chute.
In the figure, 1, a positioning assembly; 11. a slide rail; 12. a support frame; 121. a positioning rod; 122. a telescopic rod; 123. a diagonal brace; 2. a drive assembly; 21. a gear; 22. a rack; 23. a first motor; 3. a second motor; 4. a hydraulic cylinder; 41. a push plate; 42. a rubber pad; 5. a chute; 51. a slide block; 52. a spring; 6. a side wing plate; 61. a bolt; 7. a hoop; 8. a heater; 9. an evaporative crystallizer; 91. and a gas-liquid separation device.
Detailed Description
The application is described in further detail below with reference to fig. 1-4.
The embodiment of the application discloses evaporation crystallization equipment for treating high-salt wastewater.
Referring to fig. 1 and 2, an evaporative crystallization apparatus for treating high-salt wastewater includes a heater 8, an evaporative crystallizer 9, and a gas-liquid separation device 91, the heater 8 being disposed beside the evaporative crystallizer 9, the gas-liquid separation device 91 being slidably disposed on the evaporative crystallizer 9, and a sliding direction being slid in a vertical direction. The heater 8 utilizes live steam or compressor export steam to heat the feed liquid, provides suitable supersaturation degree for the crystallization of feed liquid, and evaporation crystallizer 9 alone sets up gas-liquid separation device 91 on the one hand can reduce equipment height, and on the other hand can nimble the size of adjusting gas-liquid separation device 91, guarantees the gas-liquid separation effect, and the higher the high of gas-liquid separation device 91 promptly, the better the effect of gas-liquid separation. Through the sliding component that sets up, also can change the position of gas-liquid separation device 91 relative evaporation crystallizer 9 to further satisfy wastewater treatment's demand.
Referring to FIG. 1, the amount of treated water of the evaporative crystallizer 9 is 0.5m3/h, the TDS of the incoming water is 160000mg/L, the diameter of the evaporative crystallizer 9 is 1000mm, the rising speed in the vapor-liquid separation in the evaporative crystallizer 9 is far lower than 1m/s, the lower the vapor speed is, the less the entrainment amount is, so that the height of the evaporative crystallizer 9 can be shortened when the same vapor-liquid separation effect is achieved; the diameter of the evaporating crystallizer 9 which is larger than the conventional evaporating water quantity is selected, so that the enough crystal slurry residence time can be ensured, the granularity of the crystallized salt is ensured, and the purity of the crystallized salt product is improved.
Referring to fig. 1 and 2, the heater 8 heats the feed liquid by using live steam or compressor outlet steam, the size of the heater 8 depends on the area of the heater 8 (the larger the area is, the more heat exchange tubes with the same heat exchange tube length inside the heater 8 are, and thus the diameter is large), while the area of the heater 8 is related to the effective heat transfer temperature difference (the effective heat transfer temperature difference is related to the temperature of the live steam or compressor outlet steam, the temperature of the secondary steam, and the boiling point rise of the feed liquid) and the heat exchange coefficient (the heat exchange coefficient is generally an empirical value), and only if the area of the heater 8 is suitable, the temperature rise of the feed liquid is within a suitable range (1 ℃ -2 ℃), so that a suitable supersaturation degree is provided for crystallization of the feed liquid (the supersaturation degree cannot be too large and the too large can burst to nucleate, and fine crystals are generated), and in addition, the area of the heater 8 is suitable to ensure a sufficient evaporation amount.
Referring to fig. 1, the larger the diameter of the evaporation crystallizer 9 is, the lower the rising gas velocity of the gas during gas-liquid separation is, the less entrainment is carried out, so that the quality of fresh water is improved; on the other hand, the larger the diameter is, the longer the residence time is, so that the grain diameter of the crystal is increased, and the quality of the crystal salt is improved. However, the evaporating crystallizer 9 is not suitable to be too large in diameter, which leads to an increase in the occupied area, an increase in the equipment cost and an increase in the equipment load.
Referring to fig. 1 and 3, a positioning assembly 1 is arranged on the outer wall of an evaporation crystallizer 9, the positioning assembly 1 comprises a sliding rail 11 and a supporting frame 12, the supporting frame 12 comprises two telescopic rods 122 and a positioning rod 121, the end parts, close to the positioning rods 121, of the telescopic rods 122 are fixedly connected with the positioning rods 121 to form a C shape, the positioning rods 121 are arranged on the sliding rail 11 in a sliding mode, and the sliding direction is arranged along the length direction of the sliding rail 11. The telescopic link 122 is kept away from the tip of locating lever 121 and is all fixed with staple bolt 7, and the fixed mode adopts threaded connection's mode to the staple bolt 7 of the different diameter sizes of being convenient for replace. An inclined supporting rod 123 is arranged between the two telescopic rods 122, one end of the inclined supporting rod 123 is fixedly connected with the positioning rod 121, the other end of the inclined supporting rod 123 is slidably connected with one of the telescopic rods 122, and the two telescopic rods 122 are arranged in a cross mode.
Referring to fig. 1, 3 and 4, a driving assembly 2 is disposed on a support frame 12, the driving assembly 2 includes a gear 21, a rack 22 and a first motor 23, the rack 22 is fixed on a slide rail 11, the length direction of the rack 22 is set along the length direction of the slide rail 11, the first motor 23 is fixed on the support frame 12, and at this time, the driving assembly can be fixed at the junction of two diagonal bracing rods 123, the output end of the first motor 23 is fixedly connected with the gear 21, and the gear 21 is meshed with the rack 22. The gear 21 is provided with a second motor 3 and a hydraulic cylinder 4 in a sliding manner, the gear 21 is provided with a sliding groove 5, the sliding groove 5 is formed in any diameter length direction of the gear 21, the gear 21 is provided with a spring 52, the spring 52 is positioned in the sliding groove 5, the second motor 3 is fixedly provided with a sliding block 51, the sliding block 51 slides in the sliding groove 5, the spring 52 is fixed between the sliding block 51 and the groove wall of the end part of the sliding groove 5, so that the second motor 3 slides along the direction close to or far away from the sliding rail 11, the second motor 3 is positioned on one side of the gear 21, deviating from the first motor 23, the rotating end of the second motor 3 is fixedly connected with the outer wall of the hydraulic cylinder 4, the hydraulic cylinder 4 is perpendicular to the second motor 3, namely, the output shaft of the second motor 3 is perpendicular to the piston shaft of the hydraulic cylinder 4.
Referring to fig. 1 and 3, when the positioning assembly 1 is used between the evaporative crystallizer 9 and the gas-liquid separation device 91, the sliding rail 11 is fixed on the outer wall of the evaporative crystallizer 9, the length direction of the sliding rail 11 is fixed along the vertical direction, the hoop 7 is locked on the outer wall of the gas-liquid separation device 91 in a surrounding manner, the first motor 23 is started at this time, the position of the gas-liquid separation device 91 relative to the evaporative crystallizer 9 in the vertical direction can be adjusted, the second motor 3 is started at this time, the hydraulic cylinder 4 is in a horizontal state, and the gas-liquid separation device 91 can be pushed in a direction far away from the evaporative crystallizer 9. The second motor 3 and the hydraulic cylinder 4 provided on the gear 21 are slid, so that the hydraulic cylinder 4 does not collide with the rack 22 and the slide rail 11 when the gear 21 is rotated.
Referring to fig. 1,2 and 3, when the positioning assembly 1 is used between the ground and the heater 8, the sliding rail 11 is fixed on the ground below the heater 8, the length direction of the sliding rail 11 is along the direction close to or far away from the evaporative crystallizer 9, the supporting frame 12 is slidably arranged on the sliding rail 11, the telescopic rod 122 is placed along the vertical direction, the hoop 7 is fixed on the outer wall of the heater 8 in an encircling manner, the first motor 23 is started, the horizontal distance between the heater 8 and the gas-liquid separation device 91 can be adjusted, the second motor 3 is started, and the height difference between the heater 8 and the gas-liquid separation device 91 can be adjusted. In order to ensure that the feed liquid in the heater 8 does not boil, the phenomenon of heat exchange tube drying in the heater 8 is avoided, and the height difference between the evaporation crystallizer 9 and the heater 8 which are generally designed is quite large, but in the embodiment, the total height is ensured to be within 4.2 meters, and the designed height difference is 1.2 meters based on gasification pressure data of the feed liquid, so that the feed liquid is not boiled, and the height of the device is ensured to be within 4.2 meters.
The size of the evaporation crystallizer 9 can not influence the size of the heater 8, the heater 8 can be properly sized to ensure that the temperature rise of the feed liquid is in a proper range, and then proper supersaturation degree is provided for crystallization of the feed liquid, and in addition, the area of the heater 8 is proper to ensure enough evaporation capacity.
Referring to fig. 1, a push plate 41 and a rubber pad 42 are fixed on the piston end of the hydraulic cylinder 4, the rubber pad 42 is fixedly connected with the push plate 41, and the rubber pad 42 is positioned on the side wall of the push plate 41 away from the hydraulic cylinder 4.
Referring to fig. 1 and 3, a side wing plate 6 is fixed on a supporting frame 12, a bolt 61 is arranged between the side wing plate 6 and a sliding rail 11, and the bolt 61 penetrates through the side wing plate 6 and is fixedly connected with the sliding rail 11. In the present embodiment, after the positions of the heater 8, the evaporative crystallizer 9 and the gas-liquid separation device 91 are changed, the correspondence between the communication pipes may be changed.
The implementation principle of the evaporation crystallization equipment for treating high-salt wastewater provided by the embodiment of the application is as follows: the heater 8 and the evaporative crystallization equipment are both of proper diameter sizes, the heater 8 utilizes fresh steam or steam at the outlet of the compressor to heat the feed liquid, the feed liquid is high-salt wastewater at the moment, the feed liquid is heated to proper supersaturation degree of crystallization, and then the feed liquid flows into the evaporative crystallizer 9 for evaporative crystallization; the upper position adjusting component 1 and the driving component 2 are arranged between the ground and the heater 8 and between the evaporation crystallizer 9 and the gas-liquid separation device 91, the corresponding gas-liquid separation device 91 and the heater 8 are surrounded and fixed through the anchor ear 7, the first motor 23 is started, the horizontal distance between the heater 8 and the gas-liquid separation device 91 can be adjusted, the second motor 3 is started, and the height difference between the heater 8 and the gas-liquid separation device 91 can be adjusted. In order to ensure that the feed liquid in the heater 8 does not boil, and avoid the phenomenon of heat exchange tube drying in the heater 8, the height difference between the evaporation crystallizer 9 and the heater 8 which are generally designed is quite large, but the embodiment ensures that the total height is within 4.2 meters, and the designed height difference is 1.2 meters based on gasification pressure data of the feed liquid, so that the feed liquid is not boiled, and the height of the device is within 4.5 meters; the position of the gas-liquid separation device 91 relative to the evaporative crystallizer 9 in the vertical direction can be adjusted when the first motor 23 is started, and the gas-liquid separation device 91 can be pushed to a direction far away from the evaporative crystallizer 9 when the second motor 3 is started, so that the requirements in gas-liquid separation are further met, and the gas-liquid separation effect is improved.
The embodiments of the present application are all preferred embodiments of the present application, and are not intended to limit the scope of the present application in this way, therefore: all equivalent changes in structure, shape and principle of the application should be covered in the scope of protection of the application.
Claims (10)
1. An evaporative crystallisation apparatus for the treatment of high-salt waste water, comprising a heater (8) for heating the feed liquid, characterised in that: the device comprises a heater (8), and is characterized by further comprising an evaporation crystallizer (9) connected with the heater (8), wherein a gas-liquid separation device (91) for separating a gas phase from a liquid phase is arranged on the evaporation crystallizer (9), the gas-liquid separation device (91) is arranged on the outer wall of the evaporation crystallizer (9) in a sliding manner, and the sliding direction slides along the vertical direction; the device comprises an evaporation crystallizer (9), wherein a positioning assembly (1) is arranged on the outer wall of the evaporation crystallizer (9), the positioning assembly (1) comprises a sliding rail (11) and a supporting frame (12), the sliding rail (11) is fixed on the outer wall of the evaporation crystallizer (9) along the vertical direction, the supporting frame (12) is arranged on the sliding rail (11) in a sliding manner and slides along the vertical direction, and the position, away from the sliding rail (11), of the supporting frame (12) is detachably connected with a gas-liquid separation device (91); the support frame (12) is provided with a driving component (2) for driving the support frame (12) to move on the sliding rail (11).
2. An evaporative crystallisation apparatus for the treatment of high-salt wastewater according to claim 1, characterised in that: the water treatment amount of the evaporation crystallizer (9) is 0.5m3/h, the TDS of the inflow water is 160000mg/L, the diameter of the evaporation crystallizer (9) is 1000mm, and the rising speed of the evaporation crystallizer (9) during gas-liquid separation is far lower than 1m/s.
3. An evaporative crystallisation apparatus for the treatment of high-salt wastewater according to claim 1, characterised in that: the driving assembly (2) comprises a gear (21), a rack (22) and a first motor (23), wherein the rack (22) is fixed on the sliding rail (11), the length direction of the rack (22) is set along the vertical direction, the gear (21) is rotationally arranged on the supporting frame (12), the gear (21) rotates relative to the supporting frame (12), the first motor (23) is fixed on the supporting frame (12), the output end of the first motor (23) is fixedly connected with the gear (21), and the gear (21) is meshed with the rack (22).
4. An evaporative crystallisation apparatus for treating high-salt wastewater according to claim 3, characterised in that: the gear (21) is provided with a second motor (3) and a hydraulic cylinder (4) fixedly connected with the rotating end of the second motor (3) in a sliding manner, the second motor (3) is arranged along the direction approaching or far away from the sliding rail (11), and the second motor (3) is positioned at one side of the gear (21) away from the first motor (23); the output shaft of the second motor (3) is perpendicular to the piston shaft of the hydraulic cylinder (4), the support frame (12) comprises a telescopic rod (122) and a positioning rod (121), the positioning rod (121) is in sliding connection with the sliding rail (11), and the telescopic rod (122) is used for connecting the positioning rod (121) and the gas-liquid separation device (91).
5. An evaporative crystallization apparatus for treating high salt wastewater as defined in claim 4, wherein: a sliding groove (5) is formed in the side wall of the gear (21), the sliding groove (5) is formed in any diameter and length direction of the gear (21), a sliding block (51) is fixed on the second motor (3), the sliding block (51) slides in the sliding groove (5), a spring (52) is arranged on the gear (21), and the spring (52) is fixed between the sliding block (51) and the groove wall at the end of the sliding groove (5).
6. An evaporative crystallization apparatus for treating high salt wastewater as defined in claim 4, wherein: the piston end of the hydraulic cylinder (4) is fixedly provided with a push plate (41) and a rubber pad (42) fixedly connected with the push plate (41), and the rubber pad (42) is positioned on the side wall of the push plate (41) deviating from the hydraulic cylinder (4).
7. An evaporative crystallization apparatus for treating high salt wastewater as defined in claim 4, wherein: the telescopic rods (122) are arranged at two ends of the positioning rods (121) and correspondingly distributed, inclined supporting rods (123) are arranged between the positioning rods (121) and the two telescopic rods (122), one ends of the inclined supporting rods (123) are fixedly connected with the positioning rods (121), and the other ends of the inclined supporting rods are slidably connected with the corresponding telescopic rods (122).
8. An evaporative crystallization apparatus for treating high salt wastewater as defined in claim 4, wherein: the telescopic rod (122) is far away from the end part of the locating rod (121) and is connected with a hoop (7) in a threaded mode, and the hoop (7) is used for fixing the gas-liquid separation device (91).
9. An evaporative crystallisation apparatus for treating high-salt wastewater as claimed in claim 8, wherein: the anchor ear (7) is used for fixing the heater (8) still, and slide rail (11) are fixed subaerial this moment, and support frame (12) are located between slide rail (11) and heater (8), and telescopic link (122) are used for connecting locating lever (121) and anchor ear (7).
10. An evaporative crystallisation apparatus for the treatment of high-salt wastewater according to claim 1, characterised in that: a side wing plate (6) is fixed on the support frame (12), and a bolt (61) for fixing the side wing plate (6) and the sliding rail (11) is arranged between the side wing plate and the sliding rail.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202410397330.2A CN117985800A (en) | 2024-04-03 | 2024-04-03 | Evaporation crystallization equipment for treating high-salt wastewater |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202410397330.2A CN117985800A (en) | 2024-04-03 | 2024-04-03 | Evaporation crystallization equipment for treating high-salt wastewater |
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