CN202876396U - Full-automatic scale removal multi-effect evaporator - Google Patents
Full-automatic scale removal multi-effect evaporator Download PDFInfo
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- CN202876396U CN202876396U CN 201220542838 CN201220542838U CN202876396U CN 202876396 U CN202876396 U CN 202876396U CN 201220542838 CN201220542838 CN 201220542838 CN 201220542838 U CN201220542838 U CN 201220542838U CN 202876396 U CN202876396 U CN 202876396U
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Abstract
The utility model discloses a full-automatic scale removal multi-effect evaporator. The full-automatic scale removal multi-effect evaporator comprises a heater and an evaporation chamber, wherein a particle distribution device which can enable fluid to be uniformly distributed into a heater tube nest is arranged at the bottom of the heater, and a particle separator is also arranged between the heater and the evaporation chamber. The full-automatic scale removal multi-effect evaporator adopting the technical scheme has the beneficial effects that a scale removal technology can be simplified, heat transfer is enhanced, and heat-transfer coefficients are increased, so that the evaporator can clean scales on line, and continuous production is realized. According to another preferable technical scheme of the utility model, an intensifier ring is arranged in the particle separator, the full-automatic scale removal multi-effect evaporator is also provided with the particle separator and a particle storage chamber so that liquid generates a high-speed rotating eddy to do circularly rotational motion under the effect of a centrifugal force formed by the intensifier ring when passing the cylindrical particle separator, and the rapid seperation of solid particles and the liquid is realized.
Description
Technical field
The utility model relates to evaporimeter heater tubulation internal dirt technology for eliminating field, especially relates to a kind of evaporator that adopts the solid particle automatic desludging.
Technical background
Fouling of evaporator is ubiquitous problem in the evaporating concentration process, fouling of evaporator mainly is divided into following a few class: rigid fouling, water-soluble fouling, fiber and saponified fouling, the alumina silicate fouling, scale formation mainly is to occur in the heater tubulation, and the dirt layer has weakened heat transfer greatly, reduces heat transfer coefficient, increase energy consumption, affect output and the quality of product, can affect production when serious, even cause stopping production.Existing method of removing dirt mainly is to stop to adopt after the dismounting artificial, machinery or chemical method to clean, thereby causes underproduction loss.
Therefore from last century, extensive and deep research has been carried out in this field both at home and abroad.Mostly be the change process conditions but suppress the fouling aspect, the reduction heat transfer efficiency is cost, improves energy consumption and industrial investment cost.
The utility model content
The technical problems to be solved in the utility model is, provides a kind of and can simplify stain eliminating technology, strengthens conducting heat, and increases heat transfer coefficient, so that evaporimeter full-automatic descaling evaporator of quantity-produced in the process of scale removal.
For solving the problems of the technologies described above, the technical solution adopted in the utility model is: a kind of full-automatic descaling evaporator, this evaporimeter comprises heater and vaporization chamber, and the bottom of described heater is provided with and can makes fluid well-distributing be distributed to distribution of particles device in the described heater tubulation; Also be provided with particle separator between described heater and the vaporization chamber.
Adopt the full-automatic descaling evaporator of said structure, can make fluid well-distributing be distributed to distribution of particles device in the described heater tubulation owing to be provided with in the bottom of heater, the beneficial effect of its generation is so that enter the uniform liquid that contains particle of heater and distribute and to enter in the heater tubulation, realize the at the uniform velocity perfect condition of laminar flow, prevent that middle column tube fluid flow velocity is too fast, and peripheral tubulation is excessively slow because of flow velocity, and solid particle can't pass through tubulation smoothly, causes the phenomenon of part rows duct ligation dirt.Because the random motion of solid particle is arranged, increased the shear stress of fluid to heating wall, make that the degree of supersaturation of solution reduces near the wall, delayed separating out of solute in the solution, effectively prevent the formation of dirt.Simultaneously, particle has destroyed the boundary layer, causes boiling heat transfer coefficient to increase.Fluid enters particle separator from heater upper end discharging.The separator inner fluid speed slows down, and solid particle sinks, and the realization vapour-liquid is separated admittedly.In addition, also be provided with particle separator between described heater and vaporization chamber, the separator inner fluid speed slows down, and solid particle sinks, and realizes that gas-liquid-solid separates, and the gas-liquid fluid enters vaporization chamber and evaporates, and a part of liquid recycles.
As further improvement of the utility model, be provided with intensifier ring in the described particle separator, also be provided with particle separation chamber and particle locker room, the beneficial effect of its generation is: the three-phase fluid-mixing enters the particle separation chamber from side direction, because the existence of built-in intensifier ring, allow flow rate of liquid accelerate, thereby make liquid at the eddy current that through columniform particle separation chamber the time, produces High Rotation Speed under the effect of the formed centrifugal force of intensifier ring, circulation rotatablely moves, the particle heavier than fluid is thrown to the outer wall of separation chamber, particle is slipped to collecting chamber along outer wall, and gas-liquid is flowed through and is positioned at the vortex tube of center, then flows out from outlet.
As further improvement of the utility model, described particle locker room also is provided with the particle import, and the beneficial effect of its generation is to be conducive to add for the first time the scale removal particle, and this particle import can also be arranged to install with 45 ℃ of oblique angles.
As further improvement of the utility model, described particle separator is connected by down-comer with the first import of particles circulating device, described the first import is positioned at the partially rear position, the second import top of particles circulating device, and the outlet of described particles circulating device links to each other with described heater.Adopt such structure setting, the beneficial effect of its generation is, because particle enters from the first import, circulating fluid enters from the second import, the first import is positioned at the partially rear position, the second import top of particles circulating device, like this, the liquid that the second import enters is owing to there is certain speed, can in the certain limit of import back, form negative pressure liquid stream, like this, thereby the flow velocity of the liquid that the particle that enters from the first import can enter according to the second import enters the heater from the exit with after liquid mixes again.
As further improvement of the utility model, described vaporization chamber is provided with foam catcher, be provided with the trap silk screen on the described foam catcher, the beneficial effect of its generation is: phase enters vaporization chamber, large quantity of fluid forms indirect steam and discharges from the indirect steam outlet, easily form the liquid of foam for raising because of concentration, the foam that forms during evaporation breaks after running into the trap silk screen of foam catcher.
As further improvement of the utility model, described distribution of particles device is installed in lower perforated plate 5 ~ 10mm place of the described heater of distance.Process utility model people is performing creative labour repeatedly, discovery can better realize at the uniform velocity laminar flow with lower perforated plate 5 ~ 10mm place that the distribution of particles device is installed in the described heater of distance, prevent that middle column tube fluid flow velocity is too fast, and peripheral tubulation produces because of the excessively slow phenomenon of flow velocity.
Another problem that the utility model will solve provides a kind of reduction energy consumption, economizes on resources, and evaporation rate is fast, the full-automatic scale removal multi-effect evaporator that the circulation degree is large.
For solving the problems of the technologies described above, the technical solution adopted in the utility model is that at least two unit combination of aforesaid full-automatic descaling evaporator are lined up, the beneficial effect of its generation is, saved the energy, improved the cocnentration factor of material, improved the circulation degree, evaporation rate is fast.
Description of drawings
Further describe below in conjunction with accompanying drawing and embodiment of the present utility model:
Fig. 1 is the structural representation of full-automatic descaling evaporator;
Fig. 2 is the particle separator structural representation;
Fig. 3 is cluster of grains flow schematic diagram in tubulation;
Fig. 4 is distribution of particles device structural representation;
Fig. 5 is particles circulating device structural representation;
Fig. 6 is the structural representation of full-automatic scale removal multi-effect evaporator;
Among the figure: 1, inlet, 2, lower tube box, 3, the distribution of particles device, 4, lower perforated plate, 5, heater, 6, tubulation, 7, upper perforated plate, 8, upper tube box, 9, particle separator, 10, the phase outlet, 11, the particle separation chamber, 12, the particle import, 13, the particle locker room, 14, the particles circulating device, 15, the indirect steam outlet, 16, foam catcher, 17, vaporization chamber, 18, the concentrate discharging opening, 19, circulating pump, 20, ring in the distribution of particles device, 21 distribution of particles device outer shrouds, 22, the trap silk screen, 23, steam inlet, 24, steam jet pump, 25, give birth to steam inlet, 26, the first import of particles circulating device, 27, the second import of particles circulating device, 28, the outlet of particles circulating device, 29, the second inlet, 30, the open circles porose disc.
The specific embodiment
As shown in Figure 1, inlet 1 is installed in the lowermost end of heater 5, be connected with lower tube box 2, distribution of particles device 3 is installed in about 100mm place, lower tube box 2 tops, being conducive to most the particle-liquid mixture in this position has enough distances to enter in the distribution of particles device, the evengranular distribution that makes, fluid velocity also obtains classifying rationally, make its with roughly uniformly speed enter respectively in the tubulation 6 that is installed between upper perforated plate 7 and the lower perforated plate 4, the fluid of inlet 1 is by behind the distribution of particles device 3, with middle flow velocity faster fluid well-distributing be dispersed in the peripheral tubulation, lower tube box 2 and lower perforated plate 4 are connected by flange, lower perforated plate 4 and upper perforated plate 7 middle welding tubulations 6, tubulation 6 with interior be finished to good, smooth inner wall can suppress the formation of dirt on the one hand, prevents from the other hand destroying particle because flow velocity is too fast, and upper tube box 8 also is to be connected by flange with upper perforated plate 7.
Can find out particle or the mobility status of cluster of grains in tubulation 6 from accompanying drawing 3.
In accompanying drawing 4, what be positioned at downside is the top view of distribution of particles device, upside is cross sectional representation, see significantly and find out, ring, outer shroud are divided into two parts with distributor in the distributor, and opening is distributing, and opening angle is approximately 120 degree, such structure setting avoids so that the mid portion fluid velocity is too fast, and that both sides enter the fluid velocity of tubulation 6 is excessively slow.
As shown in fig. 1, steam then enters heater 5 from steam inlet 23, also be provided with steam jet pump 24 on the steam inlet pipeline, the jet velocity and the steam pressure that are used for steam regulation, between the pipeline of steam jet pump 24 and living steam inlet 25, be connected with a pipeline, this pipeline links to each other with vaporium, and is provided with indirect steam outlet 15.
The particle-liquid mixture of process heater enters particle separator 9 from the upper tube box exit, top of heater 5, and it is middle with vaporization chamber 17 that particle separator 9 is installed in heater 5, such as Fig. 1.
As shown in Figure 2, the vapor-liquid-solid three-phase flow body enters in the particle separator 9 from the D direction, the exit that particle separator is connected with vaporization chamber 17 also is provided with the open circles porose disc 30 that the aperture is 1.5mm, directly enters in the vaporization chamber 17 from the exit in order to stop granular solids.Among Fig. 1, the three-phase fluid-mixing enters particle separation chamber 11 from side direction, particle separator is built-in with the intensifier ring (not shown), and this intensifier ring places particle separation chamber 11, and fluid is 11 formation centrifugal force in the particle separation chamber, because particle proportion is larger, enter particle locker room 13 along wall decline, phase outlet 10 is positioned at particle separator 9 upper ends, as shown in Figure 1, the phase that proportion is lighter then enters vaporization chamber 17 from stream phase outlet 10, E direction.11 lower ends, particle separation chamber are connected with particle locker room 13.Particle is mixed into heater, the F direction among Fig. 2 with the liquid that recycles after entering particles circulating device 14 by down-comer.
Shown in Figure 5 is the structural representation of particles circulating device 14, from down-comer granular solids out, the B direction of arrow, the first import 26 through the particles circulating device enters the particles circulating device, by the liquid that circulating pump 19 places come, the A direction of arrow, the second import 27 through the particles circulating device enters the particles circulating device, in the flow through outlet 28 of particles circulating device of the liquid of this mixing and granular solids, the C direction of arrow enters into heater 5.Preferably, the first import 26 of particles circulating device can be arranged on the partially rear position, the second import 27 tops of particles circulating device, as shown in Figure 5, like this, enter the liquid of particles circulating device because certain speed is arranged from the second import 27 of particles circulating device, can form certain negative pressure at the liquid periphery, thereby drive granular solids, and then mix; And the vacuum magnitude adjustment that granular solids can form according to the speed of fluid and the degree of mixing of fluid, fluid velocity is large, negative pressure is just large, just having more granular solids mixes with liquid, otherwise fluid velocity is little, and negative pressure is just little, just have fewer granular solids and mix with liquid, thereby reach granular solids and the more uniform degree of mixing of liquid.
Can with 45 degree oblique angles installations particle import 12 be set in particle locker room 13, when being convenient to use for the first time, solid particle is mouthful adding thus, as shown in fig. 1.
Phase enters vaporization chamber 17, and large quantity of fluid forms indirect steam and discharges from indirect steam outlet 15.Raise and easily form the liquid of foam for concentration, the foam that forms during evaporation breaks after running into the trap silk screen 22 of foam catcher 16.Owing to the high concentration liquid that evaporation forms, a part is from 18 dischargings of concentrate discharging opening.Another part continues circulation by circulating pump 19.
In Fig. 6, three full-automatic descaling evaporators are combined, the concentrate discharging opening of the vaporization chamber of left side evaporimeter links to each other with the second inlet of central evaporator, and the indirect steam outlet of the vaporization chamber of left side evaporimeter links to each other with the steam inlet of central evaporator; Same, the concentrate discharging opening of the vaporization chamber of central evaporator links to each other with the second inlet of right side evaporimeter, the indirect steam outlet of the vaporization chamber of central evaporator links to each other with the steam inlet of right side evaporimeter, so just formed a full-automatic scale removal multi-effect evaporator, the beneficial effect of its generation is, saved the energy, improved the cocnentration factor of material, improved the circulation degree, evaporation rate is fast.
Full-automatic descaling evaporator of the present utility model can suppress the formation of dirt effectively, according to different materials and operating mode, selects suitable particle material and form, can significantly reduce the economic loss that dirt brings in the evaporimeter.And the dirt that forms carried out on-line cleaning, and can make the thermal resistance of heat exchanger tube be controlled at lower level, strengthen heat transfer efficiency, the thermal efficiency of heater is significantly improved, reduce energy consumption.
The above is described in detail embodiment of the present utility model by reference to the accompanying drawings, but the utility model is not limited to above-mentioned embodiment, in the ken that affiliated technical field those of ordinary skill possesses, can also under the prerequisite that does not break away from the utility model aim, make a variety of changes.
Claims (7)
1. full-automatic descaling evaporator, this device comprises heater (5) and vaporization chamber (17), it is characterized in that: the bottom of described heater (5) is provided with and can makes fluid well-distributing be distributed to distribution of particles device (3) in described heater (5) tubulation; Also be provided with particle separator (9) between described heater (5) and the vaporization chamber (17).
2. full-automatic descaling evaporator according to claim 1, it is characterized in that: described particle separator is provided with intensifier ring in (9), also is provided with particle separation chamber (11) and particle locker room (13).
3. full-automatic descaling evaporator according to claim 2, it is characterized in that: described particle locker room (13) also is provided with particle import (12).
4. full-automatic descaling evaporator according to claim 1, it is characterized in that: described particle separator (9) is connected by down-comer with first import (26) of particles circulating device (14), described the first import (26) is positioned at the partially rear position, the second import (27) top of particles circulating device (14), and the outlet (28) of described particles circulating device (14) links to each other with described heater (5).
5. full-automatic descaling evaporator according to claim 1, it is characterized in that: described vaporization chamber (17) is provided with foam catcher (16), is provided with trap silk screen (22) on the described foam catcher (16).
6. each described full-automatic descaling evaporator according to claim 1 ~ 5 is characterized in that: described distribution of particles device (3) is installed in lower perforated plate (4) 5 ~ 10mm places of the described heater of distance (5).
7. full-automatic scale removal multi-effect evaporator, it is characterized in that: this multi-effect evaporator rearranges such as each described full-automatic descaling evaporator of claim 1 ~ 6 by at least two.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220542838 CN202876396U (en) | 2012-10-23 | 2012-10-23 | Full-automatic scale removal multi-effect evaporator |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201220542838 CN202876396U (en) | 2012-10-23 | 2012-10-23 | Full-automatic scale removal multi-effect evaporator |
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| CN202876396U true CN202876396U (en) | 2013-04-17 |
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| CN 201220542838 Expired - Fee Related CN202876396U (en) | 2012-10-23 | 2012-10-23 | Full-automatic scale removal multi-effect evaporator |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102921179A (en) * | 2012-10-23 | 2013-02-13 | 江苏华泰重工装备有限公司 | Full-automatic descaling multi-effect evaporator |
| CN103252103A (en) * | 2013-06-02 | 2013-08-21 | 上海亿华科技有限公司 | Evaporator and method for preventing heating chamber from being blocked during evaporation and concentration of sodium permanganate |
| CN103528415A (en) * | 2013-10-30 | 2014-01-22 | 湘潭大学 | Dirt proofing and removing and enhanced heat transferring device of circulating fluidized particles in twisted pipes |
| CN104279915A (en) * | 2013-07-09 | 2015-01-14 | 中国石油化工股份有限公司 | Solid particle ejecting distributor and online decoking device |
| CN104771922A (en) * | 2015-04-02 | 2015-07-15 | 东南大学 | Drainage device for evaporator of rotating tube bank |
| CN105344122A (en) * | 2015-09-02 | 2016-02-24 | 湖北合加环境设备有限公司 | Horizontal falling film evaporator capable of descaling in online manner |
| CN105819527A (en) * | 2016-05-12 | 2016-08-03 | 江阴市江中设备制造有限公司 | Descaling separation assembly and landfill leachate MVR evaporation device comprising same |
| CN105833563A (en) * | 2016-05-12 | 2016-08-10 | 江阴市江中设备制造有限公司 | Non-scaling heating assembly and evaporative crystallization device with same |
| CN105854339A (en) * | 2016-05-12 | 2016-08-17 | 江阴市江中设备制造有限公司 | MVR (mechanical vapor recompression) evaporative crystallizer with scale removing and preventing functions |
| CN107421347A (en) * | 2017-08-18 | 2017-12-01 | 北京必可测科技股份有限公司 | Save antiscale condenser arrangement |
-
2012
- 2012-10-23 CN CN 201220542838 patent/CN202876396U/en not_active Expired - Fee Related
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102921179B (en) * | 2012-10-23 | 2015-04-01 | 江苏华泰重工装备有限公司 | Full-automatic descaling multi-effect evaporator |
| CN102921179A (en) * | 2012-10-23 | 2013-02-13 | 江苏华泰重工装备有限公司 | Full-automatic descaling multi-effect evaporator |
| CN103252103A (en) * | 2013-06-02 | 2013-08-21 | 上海亿华科技有限公司 | Evaporator and method for preventing heating chamber from being blocked during evaporation and concentration of sodium permanganate |
| CN104279915A (en) * | 2013-07-09 | 2015-01-14 | 中国石油化工股份有限公司 | Solid particle ejecting distributor and online decoking device |
| CN103528415A (en) * | 2013-10-30 | 2014-01-22 | 湘潭大学 | Dirt proofing and removing and enhanced heat transferring device of circulating fluidized particles in twisted pipes |
| CN104771922B (en) * | 2015-04-02 | 2016-08-24 | 东南大学 | Rotating tube bank evaporator drain device |
| CN104771922A (en) * | 2015-04-02 | 2015-07-15 | 东南大学 | Drainage device for evaporator of rotating tube bank |
| CN105344122A (en) * | 2015-09-02 | 2016-02-24 | 湖北合加环境设备有限公司 | Horizontal falling film evaporator capable of descaling in online manner |
| CN105833563A (en) * | 2016-05-12 | 2016-08-10 | 江阴市江中设备制造有限公司 | Non-scaling heating assembly and evaporative crystallization device with same |
| CN105854339A (en) * | 2016-05-12 | 2016-08-17 | 江阴市江中设备制造有限公司 | MVR (mechanical vapor recompression) evaporative crystallizer with scale removing and preventing functions |
| CN105819527A (en) * | 2016-05-12 | 2016-08-03 | 江阴市江中设备制造有限公司 | Descaling separation assembly and landfill leachate MVR evaporation device comprising same |
| CN105819527B (en) * | 2016-05-12 | 2019-03-01 | 江阴市江中设备制造有限公司 | Scale removal separation assembly, the landfill leachate MVR vaporising device comprising it |
| CN107421347A (en) * | 2017-08-18 | 2017-12-01 | 北京必可测科技股份有限公司 | Save antiscale condenser arrangement |
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| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130417 Termination date: 20171023 |