CN104548651B - A kind of technical grade energy-saving and water-saving type MVR continuous evaporative crystallization system - Google Patents
A kind of technical grade energy-saving and water-saving type MVR continuous evaporative crystallization system Download PDFInfo
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- 238000002425 crystallisation Methods 0.000 title claims abstract description 42
- 230000008025 crystallization Effects 0.000 title claims abstract description 37
- 239000007788 liquid Substances 0.000 claims abstract description 72
- 230000009194 climbing Effects 0.000 claims abstract description 45
- 239000000498 cooling water Substances 0.000 claims abstract description 45
- 239000013078 crystal Substances 0.000 claims abstract description 24
- 230000003020 moisturizing effect Effects 0.000 claims abstract description 10
- 239000002994 raw material Substances 0.000 claims abstract description 10
- 239000000463 material Substances 0.000 claims description 62
- 238000010438 heat treatment Methods 0.000 claims description 16
- 230000001376 precipitating effect Effects 0.000 claims description 3
- 238000004134 energy conservation Methods 0.000 abstract description 20
- 230000000694 effects Effects 0.000 abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 14
- 239000013589 supplement Substances 0.000 abstract 1
- 238000001704 evaporation Methods 0.000 description 23
- 230000006835 compression Effects 0.000 description 22
- 238000007906 compression Methods 0.000 description 22
- 230000008020 evaporation Effects 0.000 description 22
- 238000005516 engineering process Methods 0.000 description 12
- 238000000034 method Methods 0.000 description 9
- 230000008901 benefit Effects 0.000 description 7
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- 239000006200 vaporizer Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 239000003245 coal Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- 230000004888 barrier function Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
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- 238000001556 precipitation Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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Abstract
The present invention relates to a kind of technical grade MVR continuous evaporative crystallization system. This system includes feed(raw material)inlet, moisturizing entrance, preheater, climbing film evaporator, gas-liquid separator, compressor, pipeline heater and crystal separator; Gas-liquid separator is provided with entrance, the first outlet, the second outlet and the 3rd outlet; Preheater connects climbing film evaporator by pipeline, and climbing film evaporator connects the entrance of gas-liquid separator; Compressor is connected between gas-liquid separator and climbing film evaporator by steam conveying pipe; Circulating evaporator is connected between the second outlet and entrance by pipeline, cooling water after climbing film evaporator heat exchange and the cooling water after circulating evaporator heat exchange are as the thermal source of preheater, cooling water is sent into preheater, and the cooling water outfan of preheater and moisturizing entrance are provided commonly for system water supplement; Crystal separator connects the 3rd outlet on gas-liquid separator. This system, not only cost is low, water saving, energy-conservation, joint raw material, and crystallization effect is good.
Description
Technical field
The present invention relates to a kind of with energy-conservation and water-saving result technical grade MVR continuous evaporative crystallization system.
Background technology
Function of mechanical steam recompression MechanicalVaporRecompression technology is a kind of high-efficient energy-saving environment friendly technology, is called for short MVR. Although prior art discloses a lot of MVR continuous evaporative crystallization system adopting mechanical vapor recompression technology, but in the application of technical grade, just do not seem many.
Unreasonable due to technological design, a lot of function of mechanical steam recompression continuous evaporative crystallization systems generally only have the heat supply to vaporizer of the single-stage vapor compression machine, in crystallizer part, material does not still carry out substantial amounts of heat supply, cause that the crystallization effect of existing function of mechanical steam recompression continuous evaporative crystallization system is bad, as the problems such as grain size number is tiny occur. Certainly, also there is part producer can increase jet chimney with supplementary crystalline portion heat supply, but considerably increase the complexity of MVR system, and rely on steam boiler, make MVR system break away from the dependence to steam boiler without its original significant advantage.
For these problems, publication number is a kind of function of mechanical steam recompression continuous evaporative crystallization system solving the problems referred to above and method disclosed in CN103203116A Chinese invention patent application prospectus, this function of mechanical steam recompression continuous evaporative crystallization system have employed two Mechanical Vapor Compression, and two compressors are respectively to vaporizer and crystallizer heat supply, also cooling water sensible heat has been carried out one-level recovery, for preheating, but this continuous evaporative crystallization system have employed two Mechanical Vapor Compression, the equipment cost buying two Mechanical Vapor Compression is very high, and do not have rational structure material to be heated to bubble point temperature in advance, therefore the energy consumption starting two compressors is also significantly high, structure is numerous and diverse, cause that energy-saving effect is also unsatisfactory.
In addition, existing MVR continuous evaporative crystallization system is except energy-conservation, recycling of few consideration water route, cause existing MVR continuous evaporative crystallization system continuous flow procedure to discharge and much cool down water, not only rationally recycling does not cool down the heat energy of water, prevent the pollution of cooling water, and newly need steam new in a large number to fill into, waste water resource.
Summary of the invention
The goal of the invention of the present invention is in that to provide a kind of rational technology, and cost is low, and raw material is without waste, and seriality is good, and with better energy-conservation and water-saving result technical grade MVR continuous evaporative crystallization system.
In order to realize foregoing invention purpose, present invention employs techniques below scheme:
A kind of technical grade energy-saving and water-saving type MVR continuous evaporative crystallization system, described system includes feed(raw material)inlet, moisturizing entrance, preheater, climbing film evaporator, gas-liquid separator, function of mechanical steam recompression machine, forced-circulation evaporator, pipeline heater and crystal separator; Described preheater, climbing film evaporator and forced-circulation evaporator are all heat exchange units; It all includes the material input, material outfan and the thermal source input being connected, the cooling water outfan that are connected; Described gas-liquid separator includes the entrance for sending into gas-liquid mixed material, for exporting the first outlet of steam, for the second outlet of feed liquid forced circulation and send the 3rd outlet of crystallization for feed liquid; Described feed(raw material)inlet connects the material input of preheater by pipeline, and the material outfan of preheater connects the material input of climbing film evaporator by pipeline, and the material outfan of climbing film evaporator connects the entrance of gas-liquid separator; Described function of mechanical steam recompression machine is connected between the first outlet and the thermal source input of climbing film evaporator of gas-liquid separator by steam conveying pipe, in order to shorten the vapour pressure that described gas-liquid separator exports into superheated steam and to send into climbing film evaporator, with realize material rise film heat; The material input of described forced-circulation evaporator connects the second outlet of gas-liquid separator, and the material outfan of forced-circulation evaporator is linked back the entrance of gas-liquid separator; The thermal source input of forced-circulation evaporator connects the superheated steam outfan being directly connected to the compression of function of mechanical steam recompression machine; The cooling water outfan of described climbing film evaporator and forced-circulation evaporator, connect the thermal source input of preheater each through pipeline, and cooling water is sent into preheater, in order to give the material supplementary heating flowing through in preheater; The cooling water outfan of described preheater and moisturizing entrance are connected into the compressed steam pipeline after function of mechanical steam recompression machine outfan by pipeline heater; Described crystal separator connects the 3rd outlet on described gas-liquid separator.
As preferably, described crystal separator includes connecting the entrance of the 3rd outlet on described gas-liquid separator, precipitating out crystal delivery outlet and feed liquid delivery outlet, and described feed liquid delivery outlet is connected into the material input of described forced-circulation evaporator.
As preferably, also including surge tank and cooling water conveying pump; Surge tank and cooling water conveying pump are sequentially arranged on the pipeline before the thermal source input of preheater; The cooling water outfan of described climbing film evaporator and forced-circulation evaporator all passes sequentially through surge tank and cooling water conveying pump connects preheater.
As preferably, the pipeline between the second outlet and the material input of forced-circulation evaporator of described gas-liquid separator is provided with forced circulation pump. Further, the feed liquid delivery outlet of described crystal separator is connected into the material input of forced-circulation evaporator by forced circulation pump.
Have employed the MVR continuous evaporative crystallization system of technique scheme, have the advantages that
First, this system is only with single Mechanical Vapor Compression, and compared with the continuous evaporative crystallization device of more existing employing mechanical vapor recompression technology, the Mechanical Vapor Compression that its default unit price is expensive, cost is low.
Secondly, the MVR continuous evaporative crystallization system that this system only single Mechanical Vapor Compression is set up, also the multistage recovery that indirect steam is carried out energy can be achieved, the final sensible heat regaining indirect steam and latent heat, and material entrance gas-liquid separator and crystal separator are carried out level forced circulation, forced circulation also takes full advantage of the heat of indirect steam, very energy-conservation, and it utilizes forced circulation to gas-liquid separator even crystal separator Feedback heat, thus improve crystallization effect.
Additionally, in the system of the present invention, the cooling water finally discharged in preheater is supplemented as a water resource of moisturizing porch by MVR continuous evaporative crystallization system again, thus farthest reuse heat and water.
In sum, MVR continuous evaporative crystallization system not only rational technology provided by the invention, and it is cheap to build the equipment cost religion that this VR continuous evaporative crystallization system adopts, realize water, material and heat energy without waste, it is beneficial to consecutive production, ensure the basis of continuous crystallisation has also reached good energy-conservation, water-saving result, even only need to mend a small amount of water, zero pollutant discharge.
Accompanying drawing explanation
Fig. 1: the process flow diagram of MVR continuous evaporative crystallization system in the embodiment of the present invention.
Detailed description of the invention
Below in conjunction with accompanying drawing, the present invention is described further.
Embodiment 1:
A kind of technical grade energy-saving and water-saving type MVR continuous evaporative crystallization system as shown in Figure 1, this system is mainly made up of feed(raw material)inlet 1a, moisturizing entrance 1b, preheater 2, climbing film evaporator 3,4, function of mechanical steam recompression machine 5 of gas-liquid separator, forced-circulation evaporator 7, pipeline heater 12, crystal separator 6, surge tank 13, forced circulation pump 10 and cooling water conveying pump.
As shown in Figure 1, above-mentioned with preheater 2, climbing film evaporator 3 and forced-circulation evaporator 7 mainly through heat exchange mode give flow to its interior heating material, therefore, its structure is heat exchange unit, it is respectively provided with the material input flowed into for material, flows through the material outfan having flowed out heating or evaporation in it, also there is the thermal source input flowing into thermal source and cooling water outfan, totally four ports. in Fig. 1, accompanying drawing labelling is specific as follows: the cooling water outfan 23 of the material input 20 of preheater, the material outfan 21 of preheater, the thermal source input 22 of preheater and preheater, the cooling water outfan 33 of the material input 30 of climbing film evaporator, the material outfan 31 of climbing film evaporator, the thermal source input 32 of climbing film evaporator and climbing film evaporator, the cooling water outfan 73 of the material input 70 of forced-circulation evaporator, the material outfan 71 of forced-circulation evaporator, forced-circulation evaporator thermal source input 72 and forced-circulation evaporator. and the top of above-mentioned gas-liquid separator 4 is provided with the entrance 40 for sending into gas-liquid mixture and for exporting the first outlet 41 of steam, the bottom of gas-liquid separator 4 is provided with the second outlet 42 for feed liquid forced circulation and sends the 3rd outlet 43 of crystallization for feed liquid, on the entrance 40 of gas-liquid separator 4 and under the first outlet 41, the gas-liquid separator 4 of position is provided with air filter formula drainage screen 44, air filter formula drainage screen 44 is that a stratum reticulare is high between 80-150mm, order number silk screen between 300-500 order, and air filter formula drainage screen 44 outward flange is connected with gas-liquid separator 4 inner wall sealing, upper and lower two chambers will be divided in gas-liquid separator 4.
As shown in Figure 1, above-mentioned raw materials entrance 1a connects the material input 20 of preheater 2 by pipeline, material outfan 21 pipeline of preheater 2 connects the material input 30 of climbing film evaporator 3, material flows to climbing film evaporator 3 climbing-film evaporation and sprays from its material outfan 31, and climbing film evaporator 3 connects the entrance 40 on above-mentioned gas-liquid separator 4. The feed liquid of sending of gas-liquid separator 4 exports 43 by pipeline connection crystal separator 6 entrance 60 for the 3rd of crystallization, crystal separator 6 is provided with precipitation crystal delivery outlet 61 and feed liquid delivery outlet 62, and the crystal delivery outlet 61 that precipitates out of crystal separator 6 connects holding tank 8 below.
As it is shown in figure 1, first outlet 41 input by steam conveying pipe connection Mechanical Vapor Compression 5 for exporting steam of above-mentioned gas-liquid separator 4. The outfan of Mechanical Vapor Compression 5 is connected into the thermal source input 32 of climbing film evaporator 3 by steam conveying pipe, in order to export the superheated steam that shortens into of vapour pressures of 41 outputs by the first of described gas-liquid separator and to send into climbing film evaporator 3, in climbing film evaporator 3, rise film heat realizing material. Above-mentioned forced-circulation evaporator 7 is connected between the second outlet 42 and the entrance 40 of gas-liquid separator of gas-liquid separator 4 by pipeline, specifically the second outlet 42 of the material input 70 of forced-circulation evaporator 7 and gas-liquid separator 4 is connected, and the material outfan 71 of forced-circulation evaporator 7 is linked back by pipeline the entrance 40 of liquid/gas separator. Above-mentioned forced circulation pump 10 is located on the pipeline between the second outlet 42 and the material input 70 of forced-circulation evaporator 7 of gas-liquid separator, and the feed liquid delivery outlet 62 of crystal separator 6 is connected into the material input 70 of forced-circulation evaporator 7 by forced circulation pump 10. And the thermal source input 72 of forced-circulation evaporator 7 connects the superheated steam outfan being directly connected to function of mechanical steam recompression machine 5 compression.
As shown in Figure 1, the cooling water outfan 73 of above-mentioned climbing film evaporator cooling water outfan 33 and forced-circulation evaporator connects the thermal source input 22 of preheater 2 each through pipeline, and cooling water is sent into preheater 2, in order to give the material supplementary heating flowing through in preheater 2. Specifically, above-mentioned surge tank 13 and cooling water conveying pump are sequentially arranged on the pipeline before the thermal source input 22 of preheater 2; The cooling water outfan 33 of climbing film evaporator and the cooling water outfan 73 of forced-circulation evaporator all pass sequentially through surge tank 13 and cooling water conveying pump connects preheater 2.
Finally, cool down water outfan 23 and the moisturizing entrance 1b of above-mentioned preheater 2 is connected into the compressed steam pipeline after function of mechanical steam recompression machine 5 outfan by pipeline heater 12.
Cooling water after the heat exchange of above-mentioned climbing film evaporator 3 and the cooling water after forced-circulation evaporator 7 heat exchange are the hot water with uniform temperature, also as the thermal source of preheater 2, thus energy-conservation further. Therefore, climbing film evaporator 3 cools down the cooling water outfan 73 thermal source input 22 each through pipeline connection preheater 2 of water outfan 33 and forced-circulation evaporator 7, it is therefore an objective to cooling water is sent into preheater 2 in order to the material preheating flowing through in preheater. Actually, the power consumption of every Mechanical Vapor Compression 5 use is relatively larger, if material not being heated to bubble point temperature in preheater 2, eventually after impact, film of continuing rising is heated and the compressor total power consumption to the recompression process of steam, the total energy consumption of whole continuous crystallisation device can be increased, but in order to ensure good energy saving technology effect, depend merely on cooling water not enough as the preheater 2 sometimes pre-heating temperature elevation of thermal source, therefore present invention employs the preheater 2 of electrified heating to ensure the heating material of outflow preheater 2 to bubble point temperature.
The feed liquid delivery outlet 62 of above-mentioned crystal separator is connected between forced-circulation evaporator 7 and the second outlet 42 of gas-liquid separator 4 pipeline connected, and again participates in forced-circulation evaporation, better ensures that continuous crystallisation.
As fully visible, the present invention adopts a Mechanical Vapor Compression 5 to climbing film evaporator 3 and forced-circulation evaporator 7 together steam heating, compare the equipment adopting two Mechanical Vapor Compression 5 that climbing film evaporator 3 and forced-circulation evaporator 7 are distinguished heat supply respectively, at least energy-conservation more than 20%.Why adopt a Mechanical Vapor Compression 5 to can be achieved with above-mentioned heat supply, one of reason also reside in combine present invention employs can by the preheater 2 of heating material to bubble point temperature, thus reducing the operating pressure of single Mechanical Vapor Compression 5. Consider that Mechanical Vapor Compression 5 is expensive, in the continuous evaporative crystallization equipment of existing employing mechanical vapor recompression technology, the price of Mechanical Vapor Compression 5 is to account for complete equipment price 30-50%, therefore taking cost into account, the continuous evaporative crystallization device of the present invention has the two-fold advantage that cost is low and energy consumption is low concurrently.
The above-mentioned Mechanical Vapor Compression 5 of the present embodiment is Roots Compressor, and above-mentioned climbing film evaporator 3 is pipe heat exchanger.
The following method being MVR continuous evaporative crystallization system of the present invention and carrying out continuous crystallisation, comprises the steps:
A. first, material to be crystallized is fed in preheater 2, by the sensible heat of above-mentioned cooling water as thermal source in preheater, by heating material to its bubble point temperature, but do not produce the hot solution of steam;
B. the hot solution in step a is sent in climbing film evaporator 3, climbing film evaporator 3 passes through the superheated steam after Mechanical Vapor Compression 5 compression as using, above-mentioned hot solution material is carried out heat exchange, realize rising film heating, and producing substantial amounts of indirect steam, solution is brought into gas-liquid separator 7 by indirect steam together.
In this step, the advantage that employing climbing film evaporator 3 is pipe heat exchanger is as follows: first, the expense of pipe heat exchanger unit volume is minimum in current vaporizer, secondly, compared with other vaporizers, pipe heat exchanger structure is simpler, manufactures installation requirement relatively low, finally, in the heat-transfer pipe of pipe heat exchanger, the flow velocity of indirect steam is quite fast, and between usual 20m/s 50m/s, the feed liquid time of staying is short, but total heat exchange system or relatively larger, generally can reach 1200～6009w/m2·h·℃。
Wherein solution is brought into the indirect steam of gas-liquid separator 4 process and sprays into speed between 25～50m/s by indirect steam together, in order to prevent indirect steam short circuit, during work, the air filter formula drainage screen installed in above-mentioned gas-liquid separator 4 forms one mist eliminating barrier, the liquid foam gear carried secretly by the indirect steam that material evaporation produces goes back, and only indirect steam passes through.
Consider that indirect steam sprays into speed between 25～50m/s, speed is very fast, therefore we have employed stratum reticulare height between 80-150mm, order number silk screen between 300-500 is as air filter formula drainage screen, the silk screen mist to particle diameter >=3～5um, arresting efficiency reaches 97%-98.9%, and effect is very good.
C. separating through gas-liquid separator 4, the solution of concentration exports 42 in part through gas-liquid separator 4 second and is fed again into forced-circulation evaporator 7 heating evaporation, and the gas-liquid mixture of generation returns to gas-liquid separator 4; Another part is from being expelled to crystal separator crystallization 6; In this step, indirect steam is sent gas-liquid separator and is compressed into superheated steam by function of mechanical steam recompression machine, is re-fed into climbing film evaporator 3 and forced-circulation evaporator 7 as heating energy source; Cooling water is sent into the preheater 2 part heating energy source as pre-heater by the cooling water outfan of climbing film evaporator 3 and forced-circulation evaporator 7. Cooling water and moisturizing entrance 1b that the cooling water outfan of preheater is got rid of collect jointly, and are connected into the compressed steam pipeline after function of mechanical steam recompression machine 5 outfan by pipeline heater 12. By the multistage recycling of the heat energy of this steam and water, adopting the continuous evaporative crystallization method of said system, not only production effect is good continuously, and without raw material, water waste, cost is low, but also very energy-conservation.
D. precipitating out crystal in separator crystallization 6 to discharge, residue concentrated solution also delivers to heating evaporation in the forced-circulation evaporator 7 in step c.
Embodiment 2:
Embodiment 2 and embodiment 1 are distinctive in that, the Mechanical Vapor Compression 5 of the present embodiment is centrifugal compressor, and all the other repeat embodiment 1.
Energy-conservation Experimental comparison's example:
Selection sodium carbonate is material, is added separately to by sodium carbonate in the continuous evaporative crystallization device of embodiment 1 and 2, and the method being respectively adopted embodiment 1 and 2.
The observable index of the embodiment 1 and 2 evaporating the required raw quantity of steam of 1 ton of steam multiple-effect evaporation and adopt mvr technology relatively, is shown in following form:
Table 1: the comparison of embodiment 1 and multiple-effect evaporation
Table 2: the comparison of embodiment 2 and multiple-effect evaporation
Note: according to the standard coal that heat of equal value is 0.404kg of 1kW h electricity, the standard coal that heat of equal value is 0.145kg of 1kg saturated vapor calculates
Industrial commonly using is evaporated to economic benefits and social benefits, triple effect, four-effect evaporation; It is substantially free of after five effect evaporations. One is because the multiple-effect evaporation effect more many costs of equipment of number more for huge, two be five effects after adding effect number effect and inconspicuous.
Data from table 1 can show that embodiment 1 adopts MVR technology to have comparatively significantly energy-conservation relative to tradition evaporation. Wherein compared with double-effect evaporation on average energy-conservation 78%, compared with triple effect evaporation on average energy-conservation 70%, compared with four-effect evaporation on average energy-conservation 60%, compared with five effect evaporations on average energy-conservation 55%.
Data from table 2 can show that embodiment 2 adopts MVR technology to have comparatively significantly energy-conservation relative to tradition evaporation. Wherein compared with double-effect evaporation on average energy-conservation 85%, compared with triple effect evaporation on average energy-conservation 79%, compared with four-effect evaporation on average energy-conservation 72%, compared with five effect evaporations on average energy-conservation 69%.
Claims (2)
1. a technical grade energy-saving and water-saving type MVR continuous evaporative crystallization system, it is characterised in that:
Described system includes feed(raw material)inlet (1a), moisturizing entrance (1b), preheater (2), climbing film evaporator (3), gas-liquid separator (4), function of mechanical steam recompression machine (5), forced-circulation evaporator (7), pipeline heater (12) and crystal separator (6);
Described preheater (2), climbing film evaporator (3) and forced-circulation evaporator (7) are all heat exchange units; It all includes the material input (20,30,70), material outfan (21,31,71) and the thermal source input (22,32,72) being connected, cooling water outfan (23,33,73) that are connected; Described gas-liquid separator (4) includes the entrance (40) for sending into gas-liquid mixed material, is used for exporting the first outlet (41) of steam, exports (42) for the second of feed liquid forced circulation and send the 3rd outlet (43) of crystallization for feed liquid;
Described feed(raw material)inlet (1a) connects the material input (20) of preheater (2) by pipeline, the material outfan (21) of preheater (2) connects the material input (30) of climbing film evaporator (3) by pipeline, and the material outfan (31) of climbing film evaporator (3) connects the entrance (40) of gas-liquid separator;
Described function of mechanical steam recompression machine (5) is connected between the first outlet (41) and the thermal source input (32) of climbing film evaporator of gas-liquid separator (4) by steam conveying pipe, in order to the vapour pressure that described gas-liquid separator exports is shortened into superheated steam and sends into climbing film evaporator (3), with realize material rise film heat;
The material input (70) of described forced-circulation evaporator (7) connects the second outlet (42) of gas-liquid separator, and the material outfan (71) of forced-circulation evaporator (7) is linked back the entrance (40) of gas-liquid separator; The thermal source input (72) of forced-circulation evaporator (7) is directly connected to the superheated steam outfan that function of mechanical steam recompression machine (5) compresses;
The cooling water outfan (33,73) of described climbing film evaporator (3) and forced-circulation evaporator (7) connects the thermal source input (22) of preheater (2) each through pipeline, and cooling water is sent into preheater (2), in order to give the material supplementary heating flowing through in preheater (2);
Cooling water outfan (23) and the moisturizing entrance (1b) of described preheater (2) are connected into the compressed steam pipeline after function of mechanical steam recompression machine (5) outfan by pipeline heater (12);
Described crystal separator (6) connects the 3rd outlet (43) on described gas-liquid separator (4); Described crystal separator (6) includes connecting the entrance (60) of the 3rd outlet (43) on described gas-liquid separator (4), precipitating out crystal delivery outlet (61) and feed liquid delivery outlet (62), and described feed liquid delivery outlet (62) is connected into the material input (70) of described forced-circulation evaporator (7);
Pipeline between second outlet (42) and the material input (70) of forced-circulation evaporator (7) of described gas-liquid separator is provided with forced circulation pump (10), and the feed liquid delivery outlet (62) of described crystal separator (6) is connected into the material input (70) of forced-circulation evaporator (7) by forced circulation pump (10).
2. a kind of technical grade energy-saving and water-saving type MVR continuous evaporative crystallization system according to claim 1, it is characterised in that:
Also include surge tank (13) and cooling water conveying pump; Surge tank (13) and cooling water conveying pump are sequentially arranged on the pipeline before the thermal source input (22) of preheater (2); The cooling water outfan (33,73) of described climbing film evaporator (3) and forced-circulation evaporator (7) all passes sequentially through surge tank (13) and cooling water conveying pump connects preheater (2).
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| CN106166401B (en) * | 2016-08-16 | 2018-03-16 | 广西纺源医疗科技有限公司 | Combined type barium sulfate crystallization apparatus |
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| CN201988302U (en) * | 2011-01-25 | 2011-09-28 | 杭州联合超滤净化设备有限公司 | Air water separating device |
| CN202594905U (en) * | 2012-02-23 | 2012-12-12 | 北京浦仁美华节能环保科技有限公司 | MVR (mechanical vapor recompression) efficient and energy-saving evaporating system |
| CN103203116B (en) * | 2013-04-24 | 2015-09-16 | 江苏科化节能环保设备有限公司 | A kind of MVR continuous evaporative crystallization system and continuous evaporative crystallization method |
| CN203447809U (en) * | 2013-07-05 | 2014-02-26 | 重庆江增船舶重工有限公司 | MVR (Mechanical Vapor Recompression) evaporative crystallization system |
| CN204447377U (en) * | 2015-01-19 | 2015-07-08 | 陈式好 | Technical grade energy-saving and water-saving type MVR continuous evaporative crystallization system |
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