CN106957122A - It is a kind of to be used to handle the evaporative crystallisation process of brine waste and realize the device of this method - Google Patents
It is a kind of to be used to handle the evaporative crystallisation process of brine waste and realize the device of this method Download PDFInfo
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- CN106957122A CN106957122A CN201710200466.XA CN201710200466A CN106957122A CN 106957122 A CN106957122 A CN 106957122A CN 201710200466 A CN201710200466 A CN 201710200466A CN 106957122 A CN106957122 A CN 106957122A
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- 238000000034 method Methods 0.000 title claims abstract description 87
- 230000008569 process Effects 0.000 title claims abstract description 77
- 238000002425 crystallisation Methods 0.000 title claims abstract description 71
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 55
- 239000012267 brine Substances 0.000 title claims abstract description 53
- 239000002699 waste material Substances 0.000 title claims abstract description 53
- 230000000694 effects Effects 0.000 claims abstract description 205
- 239000011552 falling film Substances 0.000 claims abstract description 191
- 239000000463 material Substances 0.000 claims abstract description 183
- 239000007788 liquid Substances 0.000 claims abstract description 96
- 238000001704 evaporation Methods 0.000 claims abstract description 88
- 230000008020 evaporation Effects 0.000 claims abstract description 76
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 63
- 239000013078 crystal Substances 0.000 claims abstract description 49
- 230000008025 crystallization Effects 0.000 claims abstract description 48
- 238000012546 transfer Methods 0.000 claims abstract description 45
- 239000012141 concentrate Substances 0.000 claims abstract description 27
- 238000009835 boiling Methods 0.000 claims abstract description 24
- 230000001965 increasing effect Effects 0.000 claims abstract description 8
- 239000007787 solid Substances 0.000 claims abstract description 6
- 239000000243 solution Substances 0.000 claims description 22
- 230000006835 compression Effects 0.000 claims description 20
- 238000007906 compression Methods 0.000 claims description 20
- 230000001105 regulatory effect Effects 0.000 claims description 18
- 239000010408 film Substances 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 9
- 239000000126 substance Substances 0.000 claims description 5
- 239000007864 aqueous solution Substances 0.000 claims description 4
- 238000010025 steaming Methods 0.000 claims description 3
- 238000010521 absorption reaction Methods 0.000 claims description 2
- 238000002347 injection Methods 0.000 claims description 2
- 239000007924 injection Substances 0.000 claims description 2
- 238000003303 reheating Methods 0.000 claims description 2
- 150000003839 salts Chemical class 0.000 abstract description 18
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 229910017053 inorganic salt Inorganic materials 0.000 description 10
- 239000002351 wastewater Substances 0.000 description 10
- 238000009833 condensation Methods 0.000 description 7
- 230000005494 condensation Effects 0.000 description 7
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 6
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 208000006558 Dental Calculus Diseases 0.000 description 5
- 230000010355 oscillation Effects 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000012266 salt solution Substances 0.000 description 4
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 150000001768 cations Chemical class 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- 229910052749 magnesium Inorganic materials 0.000 description 3
- 239000011777 magnesium Substances 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 239000003643 water by type Substances 0.000 description 3
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 150000001450 anions Chemical class 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000009102 absorption Effects 0.000 description 1
- 230000003373 anti-fouling effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000005670 electromagnetic radiation Effects 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/26—Multiple-effect evaporating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0004—Crystallisation cooling by heat exchange
- B01D9/0013—Crystallisation cooling by heat exchange by indirect heat exchange
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Thermal Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Hydrology & Water Resources (AREA)
- Life Sciences & Earth Sciences (AREA)
- Physics & Mathematics (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Crystallography & Structural Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Toxicology (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a kind of evaporative crystallisation process for being used to handle brine waste, comprise the following steps：Brine waste is passed sequentially through after electromagnetic wave launcher and one-level preheater, it is passed through in two effect falling film evaporators and is evaporated process, a concentrate after gas-liquid separator separates will be passed through by a concentrate after two effect falling film evaporator evaporations, it is passed through in an effect falling film evaporator and is evaporated crystallization, obtained secondary concentration liquid is in hypersaturated state；Secondary concentration liquid is passed through crystal separator crystallization, the liquid that crystal separator is obtained is passed through in an effect falling film evaporator again is circulated evaporation, and the crystal that crystal separator is obtained is discharged by solid discharge device.High salt concentration water evaporation crystallization process is divided into unsaturated evaporation process and supersaturated crystallization process by the present invention, ensure that material first evaporates portion of water at relatively low concentration, reduce heat transfer temperature difference in the evaporator that the supersaturated brine elevation of boiling point is brought to reduce, evaporation effect declines and the increased influence of correspondence energy consumption.
Description
Technical field：
The invention belongs to the MVR evaporation and crystallization system technical fields of industrial wastewater recycling, and in particular to Yi Zhongyong
In processing brine waste evaporative crystallisation process and realize the device of this method.
Background technology：
It is more widely used at present during the utilization of wastewater resource that the fields such as food, chemical industry and pharmacy are produced
It is MVR method of evaporating, this method has treating capacity big, efficiency high, and the advantages of applied widely, but evaporating temperature is low, heat exchange temperature
Small difference is similarly its notable feature.And high concentration salt solution vapour boiling point under hypersaturated state raises 8 DEG C~10 DEG C compared with running water,
During using conventional method single effect evaporation, material is in saturation state for a long time, and now effective heat transfer temperature difference diminishes, and causes evaporator
Evaporation efficiency declines, the increase of correspondence system energy consumption, at the same tradition MVR systems evaporation high concentration salt solution easy fouling occurs, it is frequent
The problem of maintenance shut-downs, in order to overcome disadvantage mentioned above, increase application study and raising of the MVR technologies on high-concentration salt-containing wastewater
The research of system anti-tartar.
The content of the invention：
It is an object of the invention to provide it is a kind of be used for handle brine waste evaporative crystallisation process and realize this method
Device, material liquid is crystallized through two-effect evaporation, and the first effect evaporation process feed concentration is relatively low, and saturation state is reached far away, this
Boiling point liter can be ignored under state, first evaporate part moisture, and during do not produce crystal salt, the effect evaporation process is effective
Heat transfer temperature is big, and evaporation efficiency is high；Concentrated solution after evaporation is steamed again after being mixed again with supersaturated solution in 2nd effect evaporator
Boiling point rises higher under hair, this state, while occurring crystallization process, it is thus possible to improve overall evaporation efficiency, reduces high salt concentration
Water evaporation crystallizes energy consumption.
First purpose of the present invention is to provide a kind of evaporative crystallisation process for being used to handle brine waste, including following step
Suddenly：
(1) brine waste is passed sequentially through after electromagnetic wave launcher and one-level preheater, brine waste be preheated to low
In 1 DEG C~3 DEG C of the corresponding saturation temperature of pressure in two effect falling film evaporators, be passed through in two effect falling film evaporators be evaporated it is dense
Contracting, the material of the process is in unsaturated state, will be passed through gas-liquid by a concentrate after two effect falling film evaporator evaporations
Separator is separated, and after gas-liquid separator separates a concentrate is heated to less than an effect falling liquid film by material reheater
1 DEG C of the corresponding saturation temperature of evaporimeter internal pressure~3 DEG C, is passed through in an effect falling film evaporator and is evaporated crystallization, in an effect
The secondary concentration liquid obtained in falling film evaporator after evaporative crystallization is in hypersaturated state, and supersaturated solution boiling point now is higher than
The boiling point of the aqueous solution under one effect falling film evaporator corresponding pressure；Secondary concentration liquid is passed through crystal separator Crystallization Separation, tied
The concentrated solution for the saturation state that brilliant separator is obtained is passed through in an effect falling film evaporator and is evaporated again, and crystal separator is obtained
Crystal discharged by solid discharge device；
(2) brine waste enters an effect falling film evaporator, two effect falling film evaporations after two effect falling film evaporators are concentrated by evaporation
Steam of the concentrate of device after gas-liquid separator separates is boosted by vapour compression machine, after being boosted through vapour compression machine
Thermal source of the effect falling film evaporator as an effect falling film evaporator is passed through, what is obtained after an interior evaporation of effect falling film evaporator is secondary dense
The steam obtained in the crystallized separator of contracting liquid, process is evaporated as the thermal source of two effect falling film evaporators.
The present invention is for evaporator surface inorganic salts fouling feature in the brine waste evaporation and crystal process of high concentration, in thing
Oscillating electromagnetic wave transmitting device is set up at the material entrance mouth of pipe, 120~150KHz sine wave signal is produced, is spread all over along material medium
Whole system, electromagnetic wave charges in solution for charged particle, and the cation such as calcium, magnesium and sulfate, carbonate etc. in water is negative
Ions binding is washed away into crystal with current, it is impossible in fouling on heat exchange tube wall, so that the anti-tartar of present system is improved, at this
In invention, oscillating electromagnetic wave transmitting device is higher-order of oscillation electromagnetic wave transmitter.
The evaporative crystallisation process of processing brine waste proposed by the present invention specifically includes following steps：
(1) that Inorganic salt is passed sequentially through into electromagnetic wave launcher, one-level in (5 ± 1) % brine waste is pre-
Hot device and two grades of preheaters are preheating to 1 DEG C~3 DEG C (such as two less than the corresponding saturation temperature of pressure in two effect falling film evaporators
It is 47.4Kpa to imitate pressure in falling film evaporator, and correspondence evaporating temperature is 80 DEG C, then the brine waste after two grades of preheater preheatings
Temperature be 78 DEG C), be passed through in two effect falling film evaporators and be evaporated concentration, the material of the process is in unsaturated state, general
Gas-liquid separator is passed through by a concentrate after two effect falling film evaporator evaporations to be separated, now a concentrate is inorganic
Salt content is in (9 ± 1) %, and the elevation of boiling point is not obvious, and a concentrate after gas-liquid separator separates passes through material reheater
(such as pressure is be heated to less than the corresponding saturation temperature of pressure in 1st effective evaporator 1 DEG C~3 DEG C in one effect falling film evaporator
70.1Kpa, correspondence evaporating temperature is 90 DEG C, then the temperature of the brine waste after two grades of preheater preheatings is 88 DEG C), it is passed through one
Crystallization is evaporated in effect falling film evaporator, after gas-liquid separator separates a concentrate is in an effect falling film evaporator
The secondary concentration liquid obtained after evaporative crystallization is in hypersaturated state, and Inorganic salt is more than 35%, supersaturation now
Solution boiling point is higher than the boiling point of the aqueous solution under corresponding pressure, the elevation of boiling point (8 ± 1) DEG C；Secondary concentration liquid is passed through crystallization
Separator Crystallization Separation, the concentrated solution for the saturation state that crystal separator is obtained is passed through in an effect falling film evaporator again is steamed
Hair, the crystal that crystal separator is obtained is discharged by solid discharge device；
(2) high concentration inorganic salt wastewater enters an effect falling film evaporator, two effects after two effect falling film evaporators are concentrated by evaporation
Evaporating temperature is 80 DEG C under pressure in falling film evaporator, and a concentrate of two effect falling film evaporators passes through gas-liquid separator separates
Steam afterwards boosts to 130Kpa or so by vapour compression machine, and the lower saturation temperature of pressure correspondence is 106 DEG C, is passed through an effect
Falling film evaporator is as the thermal source of an effect falling film evaporator, and the secondary concentration liquid obtained after an interior evaporation of effect falling film evaporator is through knot
The steam obtained in brilliant separator, is evaporated process, now as the steam of thermal source as the thermal source of two effect falling film evaporators
Temperature is (90 ± 1) DEG C or so.High salt concentration water evaporation crystallization process is divided into unsaturated evaporation process and supersaturation by the present invention
Evaporation process in crystallization process, i.e., two effect falling film evaporators is the evaporation in unsaturated evaporation process, an effect falling film evaporator
Process is supersaturated crystallization process, it is ensured that material first evaporates portion of water at relatively low concentration, reduces supersaturated salt
Heat transfer temperature difference reduces in the evaporator that water boiling point elevated band is come, and evaporation effect declines and the increased influence of correspondence energy consumption.
Preferably, brine waste is passed sequentially through into electromagnetic wave launcher, one-level preheater and two grades of preheatings in step (1)
After device, evaporation in two effect falling film evaporators is passed through.Normal temperature brine waste enters one-level preheater, material outlet point by product pump
Into two-way, two grades of preheaters are entered all the way and continue to preheat, another road is directly entered two effect falling film evaporators and is directly evaporated, thing
Whether material needs two grades of preheaters to continue to preheat, and may determine whether to need two grades by the closing of regulating valve according to actual conditions
Preheater is preheated.
Preferably, the high-temperature condensation water that the steam in a described effect falling film evaporator is produced after being heated as thermal source passes through
Material reheater discharges a part of heat, still with higher temperature, enters back into one-level preheater and is preheated, with cryogenic condensation
Outside the mode discharge system of water.
Preferably, the condensed water that the steam in two described effect falling film evaporators is produced after being heated as thermal source is directly arranged
Go out, or the condensed water enters after two grades of preheater heat absorptions, then the condensed water is discharged.A condensed water part for 2nd effect evaporator
Preheated into two grades of preheaters, a part is expelled directly out system, regulation enters the temperature of charge of two effect falling film evaporators.
It is a further object to provide a kind of device for realizing the evaporative crystallisation process for handling brine waste,
Including electromagnetic wave launcher, one-level preheater, two grades of preheaters, two effect falling film evaporators, gas-liquid separator, material reheating
Device, an effect falling film evaporator and crystal separator, one-level preheater are connected with first material transfer pipeline, described electromagnetic wave hair
Injection device is arranged on first material transfer pipeline, and described one-level preheater and two grades of preheaters pass through second material delivery pipe
Road is connected, and described one-level preheater and two effect falling film evaporators are connected by 3 material transfer pipeline, the second described thing
Material conveying tube road and 3 material transfer pipeline are connected in parallel, and two described effect falling film evaporators and gas-liquid separator pass through the 4th
Material delivery pipe road is connected, and described gas-liquid separator is connected with material reheater by the 5th material delivery pipe road, described
Material reheater and an effect falling film evaporator are connected by the 6th material delivery pipe road, a described effect falling film evaporator and crystallization
Separator is connected by the 7th material delivery pipe road；A described effect falling film evaporator bottom is provided with first material outlet, one
Primary concentration liquid in effect falling film evaporator is delivered to through first material outlet by the 8th material delivery pipe road is arranged at an effect
First material entrance at the top of falling film evaporator, makes primary concentration liquid be crystallized in an effect falling film evaporator, two described effect drops
The brine wastes that film evaporator bottom is provided with second material outlet, two effect falling film evaporators pass through the through second material outlet
Nine material delivery pipe roads are delivered to the second material entrance being arranged at the top of two effect falling film evaporators, make brine waste in two effect drops
Evaporated in film evaporator；The first steam (vapor) outlet is provided with the top of gas-liquid separator, the steam in gas-liquid separator is passed through first
Steam pipework is delivered to vapour compression machine, steam is increased to the temperature and pressure specified, then convey by the second steam pipework
To an effect falling film evaporator as thermal source, crystal separator top is provided with the second steam (vapor) outlet, by the steaming in crystal separator
Vapour is delivered to the first steam inlet being arranged on the outside of two described effect falling film evaporators, two effect falling liquid films by the 3rd steam pipework
Second steam inlet of evaporator is connected by the 4th steam pipework with steam generator.
Steam generator is that system supplements steam and startup steam by the 4th steam pipework.Electromagnetic wave launcher and
One material delivery pipe road is connected, and is charged in solution for charged particle, by the cation such as calcium, magnesium in water and sulfate, carbonate
It is combined into crystal Deng anion and is washed away with current, it is impossible in fouling on heat exchange tube wall.
High-frequency electromagnetic wave transmitting device is installed at material inlet, the two-way higher-order of oscillation electromagnetic wave of generation is along material flow
Be delivered to whole system, stage falling-film evaporators can be prevented, in two grades of falling film evaporators during phase-change heat-exchange sulfate and
The formation of carbonate scale, improves the anti-tartar of evaporation and crystallization system.Two effect falling film evaporators pass through gas-liquid separator and vapour pressure
Contracting machine inlet communication, forms subnormal ambient evaporation.
Two effect falling film evaporator concentrated solution material outlets are connected with material reheater heat side, an effect falling film evaporator condensation
Water out is connected with material reheater heated side, and the material after concentration is heated and the supersaturated salt in effect falling film evaporator bottom again
Solution is mixed.
Preferably, the first condensation-water drain of described effect falling film evaporator successively with described material reheater and one
Level preheater is connected by the first condensate line and the second condensate line, and the second of two described effect falling film evaporators condense
Water out is connected with the condensing water inlet of water tank by the 4th condensate line, the 3rd condensation-water drain of described water tank
Connected with two grades of preheaters by the 5th condensate line, the second condensation-water drain of described two effects falling film evaporators passes through the
Three condensate lines are connected with condensate drain outlet, the 3rd described condensate line and described the 4th condensate line parallel connection
Connection.Two effect falling film evaporator condensed water sides connects with water tank, and are provided with bypass and directly outside removal system, can be passed through change
Two grades of material preheater heated side waters, reach the purpose of regulation 1st effective evaporator material inlet temperature.
Preferably, described crystal separator bottom is provided with liquid delivery tube, and described liquid delivery tube is highly higher than
Highly, described liquid delivery tube is connected by the tenth material delivery pipe road with the 8th described material delivery pipe road for the stacking of crystal
It is logical.The height of liquid delivery tube higher than crystal stacking highly, it is ensured that liquid does not have the entrance of crystal, liquid heat again with
One effect falling film evaporator bottom supersaturated salt solution mixing, is delivered in an effect falling film evaporator by the 8th material delivery pipe road
Evaporation.
Preferably, it is provided with regulation mass flow in described second material transfer pipeline and 3 material transfer pipeline
Material is provided with second regulating valve and the 3rd regulating valve, the 8th described material delivery pipe road and the 9th material delivery pipe road
Circulating pump.
Preferably, the 4th regulating valve of regulation steam flow is provided with the 4th described steam pipework.
The beneficial effects of the invention are as follows：
1st, handle that there is provided a kind of unit work consumptiom is low, evaporation efficiency using MVR technical resourceizations for high-concentration salt-containing wastewater
The strong method of high, antifouling capability；
2nd, using single-stage point effect evaporative crystallisation process, concentrated salt solution and grain of salt crystals can be obtained simultaneously；
3rd, double-effect evaporation process is realized using a vapour compression machine, system architecture is simple, and cost of investment is low, market prospects
It is wide；
4th, higher-order of oscillation electromagnetic wave launcher is installed additional, enhancing present system is to inorganic salts such as carbonate, sulfate
Anti-tartar；
5th, by evaporative crystallization separation process, the high-salt wastewater that the industry such as chemical industry, food is produced reaches discharging standards,
Inorganic salt particle is reclaimed simultaneously, brings extra returns.
Brief description of the drawings：
Fig. 1 realizes the schematic device of the evaporative crystallisation process for handling brine waste for the present invention；
Description of reference numerals：1st, one-level preheater；2nd, two grades of preheaters；3rd, water tank；4th, two effect falling film evaporator；5th, gas
Liquid/gas separator；6th, Roots's vapour compression machine；7th, high-frequency electromagnetic wave launcher；8th, material reheater；9th, an effect falling film evaporator；
10th, crystal separator；11st, steam generator；12nd, first material transfer pipeline；13rd, second material transfer pipeline；14th, the 3rd thing
Material conveying tube road；15th, 4 materials transfer pipeline；16th, the 5th material delivery pipe road；17th, the 6th material delivery pipe road；18th,
Seven material delivery pipe roads；19th, the 8th material delivery pipe road；20th, the 9th material delivery pipe road；21st, the tenth material delivery pipe road；
22nd, the first steam pipework；23rd, the second steam pipework；24th, the 3rd steam pipework；25th, the 4th steam pipework；26th, the first condensed water
Pipeline, the 27, second condensate line；28th, the 3rd condensate line；29th, the 4th condensate line；30th, the 5th condensate line；
31st, the first regulating valve；32nd, the second regulating valve；33rd, the 3rd regulating valve；34th, the 4th regulating valve；35th, first material pump；36th, second
Matter Transfer pump；37th, 3 material pump；38th, 4 materials circulating pump.
Embodiment：
Following examples are that the present invention is further illustrated, rather than limitation of the present invention.
Except special instruction, experimental facilities and reagent in the present invention are the conventional commercial products of the art.Adjusted in Fig. 1
Valve QV01, QV02, QV03, QV04, QV05, QV06, QV07, QV08, QV09, QV10, QV11 and QV12 are saved, label is in order to just
In the installation site and purposes of distinguishing each regulating valve, each regulating valve is the same model, as long as the regulating valve can meet real
The need for border；Product pump P01, P02, P03, P04, P05 and P06 label is for the ease of distinguishing the installation of each product pump
Position and purposes, wherein P02 and P04 are Matter Transfer pumps, and remaining is conventional material-handling pump or met at actual
The need for the flow of reason, when SG01 is that crystal grain is to specified altitude assignment in feeding valve, Crystallization Separation tank, valve, discharge are opened
Inorganic salt particle.Arrow in Fig. 1 represents the flow direction of material, condensed water or steam.
The evaporative crystallisation process proposed by the present invention for being used to handle brine waste is concretely comprised the following steps：
(1) inorganic salt content is passed sequentially through into electromagnetic wave launcher, one-level preheater in (5 ± 1) % brine waste
1 DEG C~3 DEG C (such as two effect falling liquid films of saturation temperature corresponding less than pressure in two effect falling film evaporators are preheating to two grades of preheaters
Evaporimeter internal pressure is 47.4Kpa, and correspondence evaporating temperature is 80 DEG C), it is passed through in two effect falling film evaporators and is evaporated concentration, should
The material of process is in unsaturated state, will be passed through gas-liquid separator by a concentrate after two effect falling film evaporator evaporations
Separated, now a concentrate inorganic salt content is in (9 ± 1) %, and the elevation of boiling point is not obvious, after gas-liquid separator separates
A concentrate 1 DEG C~3 DEG C less than the corresponding saturation temperature of pressure in 1st effective evaporator are heated to by material reheater
(such as one effect falling film evaporator pressure is 70.1Kpa, and correspondence evaporating temperature is 90 DEG C), is passed through in an effect falling film evaporator and is steamed
Hair crystallization, it is secondary that a concentrate after gas-liquid separator separates is obtained in an effect falling film evaporator after evaporative crystallization
Concentrate is in hypersaturated state, and mass concentration is more than 35%, and supersaturated solution boiling point now is higher than under corresponding pressure
The aqueous solution, the elevation of boiling point (8 ± 1) DEG C；Secondary concentration liquid is passed through crystal separator Crystallization Separation, it is full that crystal separator is obtained
It is passed through in an effect falling film evaporator and is evaporated again with the concentrated solution of state, the crystal that crystal separator is obtained is arranged by solid
Put device discharge；
(2) high concentration inorganic salt wastewater enters an effect falling film evaporator, two effects after two effect falling film evaporators are concentrated by evaporation
Evaporating temperature is 80 DEG C under pressure in falling film evaporator, and a concentrate of two effect falling film evaporators passes through gas-liquid separator separates
Steam afterwards boosts to 130Kpa or so by vapour compression machine, and corresponding saturation temperature is 106 DEG C under the pressure, is passed through one
Imitate the secondary concentration liquid warp obtained after being evaporated in thermal source of the falling film evaporator as an effect falling film evaporator, an effect falling film evaporator
The steam obtained in crystal separator, is evaporated process, now as the steaming of thermal source as the thermal source of two effect falling film evaporators
Stripping temperature is in (90 ± 1) DEG C.
Realize the device of the evaporative crystallisation process for handling brine waste, including the preheating of electromagnetic wave launcher, one-level
Device, two grades of preheaters, two effect falling film evaporators, gas-liquid separator, material reheater, one imitate falling film evaporator and Crystallization Separation
Device, one-level preheater is connected with first material transfer pipeline, and electromagnetic wave launcher is arranged on first material transfer pipeline, and one
Level preheater and two grades of preheaters are connected by second material transfer pipeline, and one-level preheater and two effect falling film evaporators pass through the
3 material transfer pipeline is connected, and second material transfer pipeline and 3 material transfer pipeline are connected in parallel, two effect falling film evaporators
Connected with gas-liquid separator by 4 materials transfer pipeline, gas-liquid separator and material reheater pass through the 5th material delivery pipe
Road is connected, and material reheater and an effect falling film evaporator are connected by the 6th material delivery pipe road, an effect falling film evaporator and knot
Brilliant separator is connected by the 7th material delivery pipe road；One effect falling film evaporator bottom is provided with first material outlet, an effect drop
Primary concentration liquid in film evaporator is delivered to be arranged at the top of an effect falling film evaporator by the 8th material delivery pipe road
One material inlet, makes primary concentration liquid be crystallized in an effect falling film evaporator, two effect falling film evaporator bottoms are provided with the second thing
Brine waste in material outlet, two effect falling film evaporators is delivered to by second material outlet by the 9th material delivery pipe road to be set
The second material entrance being placed at the top of two effect falling film evaporators, makes brine waste be evaporated in two effect falling film evaporators；Gas-liquid point
From the first steam (vapor) outlet is provided with the top of device, the steam in gas-liquid separator is delivered to both vapor compression by the first steam pipework
Machine, steam is increased to the temperature and pressure specified, then is delivered to an effect falling film evaporator by the second steam pipework and be used as heat
The second steam (vapor) outlet is provided with the top of source, crystal separator, the steam in crystal separator is conveyed by the 3rd steam pipework
To the first steam inlet being arranged on the outside of two described effect falling film evaporators, the second steam inlet of two effect falling film evaporators leads to
The 4th steam pipework is crossed to connect with steam generator.
Embodiment 1
High-concentration salt-containing wastewater is handled using device as shown in Figure 1, is comprised the following steps：
(1) the Nacl waste water for producing the industries such as chemical industry, food, mass concentration 5%, pass sequentially through electromagnetic radiation dress
Put, tentatively preheated into one-level preheater 1 after first material transfer pipeline 12, then entered by second material transfer pipeline 13
Enter two grades of preheaters, be heated to 78 DEG C, be then passed through by 3 material transfer pipeline 14 in two effect falling film evaporators 4 and bottom
It is evaporated after material mixing, pressure is 47.4Kpa in two effect falling film evaporators, the mass concentration of material is up to 9.5%, this process
Material is constantly under low concentration state, and material boiling point is identical with light water, then will by two effect falling film evaporators 4 evaporate after
One time concentrate is passed through gas-liquid separator 5 by 4 materials transfer pipeline 15, and a concentrate is passed through into 5 points of gas-liquid separator
From a concentrate after being separated through gas-liquid separator 5 is heated to by the 5th material delivery pipe road 16 in material reheater 8
88 DEG C, a concentrate after being heated by material reheater 8 is passed through an effect falling liquid film by the 6th material delivery pipe road 17 and steamed
Progress evaporative crystallization is mixed in hair device 9 with supersaturated feed liquid, an effect falling film evaporator pressure is 70.1Kpa, obtains secondary concentration
The mass concentration of material is more than 35%, and the material of the evaporation process in the stage is constantly in hypersaturated state, now secondary dense
Contracting feed liquid boiling point is upgraded to 6 DEG C, and secondary concentration liquid is passed through into crystal separator 10 by the 7th material delivery pipe road 18 crystallizes, crystallization
The liquid that separator 10 is obtained is passed through in an effect falling film evaporator 9 and is evaporated again by the tenth material delivery pipe road, crystallization
The crystal that separator 10 is obtained is discharged by solid discharge device；Two effect falling film evaporator 4 bottoms are provided with second material outlet,
Brine waste in two effect falling film evaporators 4 is delivered to through second material outlet by the 9th material delivery pipe road 20 is arranged at two
The second material entrance at the top of falling film evaporator 4 is imitated, brine waste is evaporated in two effect falling film evaporators 4；One effect falling liquid film steams
Hair device 9 bottom is provided with primary concentration liquid in first material outlet, an effect falling film evaporator through first material outlet by the
Eight material delivery pipe roads 19 are delivered to the first material entrance for being arranged at the top of an effect falling film evaporator 9, primary concentration liquid is existed
Evaporated in one effect falling film evaporator 9；
(2) steam produced through steam generator 11 is passed through in two effect falling film evaporators 4 by the 4th steam pipework 25, is made
Enter two effect falling film evaporators 4 for device startup steam, be used as heat of the brine waste when two effect falling film evaporators 4 evaporate
Source, the heated side steam inlet temperature of two effect falling film evaporators 4 is set as 90 DEG C, after two effect falling film evaporators 4 evaporate
Steam of the concentrate after the separation of gas-liquid separator 5, about 80 DEG C are passed through both vapor compression by the first steam pipework 22
In machine, 106 DEG C or so are warming up to, corresponding pressure is 132.4Kpa, are compressed vapour compression machine by the second steam pipework 23
Steam is passed through in thermal source of the effect falling film evaporator 9 as an effect falling film evaporator 9, an effect falling film evaporator 9 and obtained after evaporation afterwards
To the crystallized separator 10 of secondary concentration liquid in obtain steam, about 90 DEG C, the steam obtained in crystal separator 10 is led to
Cross the 3rd steam pipework 24 be passed through two effect falling film evaporators as two effect falling film evaporators 4 thermals source be evaporated, until two effect
The effect falling film evaporator 9 of falling film evaporator 4 and one reaches after the pressure of setting that steam off generator 11 is switched, and system enters
The normal evaporative crystallization stage.
High salt concentration water evaporation crystallization process is divided into unsaturated evaporation process and supersaturated crystallization process, i.e., two by the present invention
It is that the evaporation process in unsaturated evaporation process, an effect falling film evaporator is tied for supersaturation to imitate the evaporation process in falling film evaporator
Brilliant process, it is ensured that material first evaporates portion of water at relatively low concentration, reduces the supersaturated brine elevation of boiling point and brings
Evaporator in heat transfer temperature difference reduce, evaporation effect declines and correspondence energy consumption increased influence.Material liquid (brine waste) is through two
Crystallized after effect evaporation, the first effect evaporation process feed concentration is relatively low, and saturation state is reached far away, and boiling point liter can under this state
To ignore, first evaporate part moisture, and during do not produce crystal salt, the effective heat transfer temperature of effect evaporation process is big, steams
Send out efficiency high；Concentrated solution after evaporation is evaporated again after being mixed again with supersaturated solution in 2nd effect evaporator, is boiled under this state
Point rises higher, while occurring crystallization process.It is thus possible to improve overall evaporation efficiency 30%, reduces high salt concentration water evaporation knot
Brilliant energy consumption.
In the present embodiment, electromagnetic wave launcher is high-frequency electromagnetic wave launcher 7, and high-frequency electrical is installed at material inlet
Magnetic wave emitter, produces 120~150KHz sine wave signal, and the two-way higher-order of oscillation electromagnetic wave of generation is passed along material medium
All over whole system, electromagnetic wave charges in solution for charged particle, promotes the cations such as calcium in water, magnesium and sulfate, carbonate
Be combined into crystal Deng anion and washed away with current, it is impossible to the fouling on heat exchange tube wall, can prevent stage falling-film evaporators, two grades
In falling film evaporator during phase-change heat-exchange sulfate and carbonate scale formation, improve evaporation and crystallization system anti-tartar.
Two effect falling film evaporators 4 form subnormal ambient evaporation by gas-liquid separator 5 and vapour compression machine inlet communication；
One effect falling film evaporator 9 and vapour compression machine outlet, one-level is ensured by compressed steam, control liquid level and installation discrepancy in elevation etc.
The pressure environment of falling film evaporator 9.
Brine waste after one-level preheater 1, which is passed through in two effect falling film evaporators 4, to be evaporated, if passing through one-level after measured
Brine waste temperature after preheater 1 is preheated is not up to assigned temperature, will can again be passed through by the brine waste of one-level preheater 1
3 material transfer pipeline 14 is after the preheating of two grades of preheaters 2 reaches assigned temperature, then is passed through in two effect falling film evaporators 4
Evaporation.
The one effect material outlet of falling film evaporator 9 is connected with the heat side of material reheater 8, an effect condensed water of falling film evaporator 9
Outlet is connected with the heated side of material reheater 8, and the material after concentration is heated and the supersaturated salt in effect falling film evaporator 9 bottom again
Solution is mixed.
In the present embodiment, vapour compression machine is Roots's vapour compression machine 6, and it can meet the need of raise steam in system
Ask.First condensation-water drain of one effect falling film evaporator 9 passes through the first condensation with material reheater 8 and one-level preheater 1 successively
Water lines 26 are connected with the second condensate line 27, the condensation of the second condensation-water drain and water tank 3 of two effect falling film evaporators 4
Water inlet is connected by the 4th condensate line 29, and the 3rd condensation-water drain and two grades of preheaters 2 of water tank 3 are cold by the 5th
Condensate line 30 is connected, and the second condensation-water drain of two effect falling film evaporators 4 is arranged by the 3rd condensate line 28 and condensed water
Mouth connection is put, the 3rd condensate line 28 and the 4th condensate line 29 are connected in parallel.The two effect condensation-water drains of falling film evaporator 4
Connected with water tank 3, and, by changing two grades of heating waters of preheaters 2, tune can be reached directly outside removal system provided with bypass
Section one imitates the purpose of the material inlet temperature of falling film evaporator 9.
The bottom of crystal separator 10 is provided with liquid delivery tube, the height of liquid delivery tube higher than crystal stacking highly,
Ensure that liquid does not have the entrance of crystal, liquid delivery tube passes through the tenth material delivery pipe road 21 and the 8th material delivery pipe road 19
Blending transportation evaporates into an effect falling film evaporator 9.
In the present invention, first material transfer pipeline 12, second material transfer pipeline 13,3 material transfer pipeline 14,
4 materials transfer pipeline 15, the 5th material delivery pipe road 16, the 6th material delivery pipe road 17, the 7th material delivery pipe road 18,
It can be set in 8th material delivery pipe road 19, the 9th material delivery pipe road 20 and the tenth material delivery pipe road 21 according to actual conditions
It is equipped with the regulating valve and the product pump beneficial to Flow of Goods and Materials of regulation mass flow.In the present embodiment, second material transfer pipeline
It is provided with 13 on second regulating valve 32,3 material transfer pipeline 14 and is provided with the 3rd regulating valve 33, the 5th material delivery pipe
It is provided with road 16 on 3 material pump 37, the 8th material delivery pipe road 19 and is provided with 4 materials circulating pump 38, the 9th material
Second material circulating pump 36 is provided with transfer pipeline 20, using forced circulation pump, it is ensured that material steams in evaporator interior circulation
Setting concentration or circulation crystallization are sent to setting state.
First condensate line 26, the second condensate line 27, the 3rd condensate line 28, the and of the 4th condensate line 29
The water pump that in 5th condensate line 30 regulating valve can be set according to actual conditions and flowed beneficial to condensed water.
It is proposed by the present invention be applied to processing brine waste the technological process of evaporative crystallisation process be：Normal temperature stoste passes through
First material circulating pump (P01) 35 enters one-level preheater 1, and brine waste outlet is divided into two-way, all the way into two grades of preheaters 2
Continue to preheat, another road is directly entered two effect falling film evaporators 4 and is directly evaporated, is adjusted according to feeding temperature and concentration
Ensure to enter two effect falling film evaporator temperature of charge close to evaporating temperature.Brine waste is a concentrate after evaporating for the first time,
Concentrate concentration increase, the dense feed liquid after being separated through gas-liquid separator 5 is heated again into material reheater 8, after heating
Into an effect falling film evaporator 9, occurs crystallization process in an effect falling film evaporator 9, the feed liquid of fractional saturation state is through the 4th thing
Expect that circulating pump (P02) 38 enters to continue to evaporate in an effect falling film evaporator 9, part feed liquid carries crystal salt and enters crystal separator
10, inorganic salt particle recovery is isolated, remaining dense feed liquid imports the dense material in the bottom of 2nd effect evaporator 4 by lower liquid delivery pipe
Liquid pipe road circulating and evaporating again.
The steam of gas-liquid separator 8 enters an effect falling film evaporation after the increasing temperature and pressure of lobed rotor compressor 6 as primary steam
Device 9 is evaporated crystallization process, and this process is in the steam produced in normal pressure state, evaporation and crystal process and entered as thermal source
2nd effect evaporator 4 carries out the evaporation process of unsaturated solution, and this process is in negative pressure state.
The high-temperature condensation water of one effect falling film evaporator 9 enters material reheater 8 and releases partial heat, still with higher temperatures
Degree, enters back into one-level preheater 1 and is preheated, in the way of cryogenic condensation water outside discharge system.
The condensed waters of two effect falling film evaporators 5 are partly into two grades of preheaters 2 and preheated, a part be expelled directly out be
System, regulation enters the temperature of charge of two effect falling film evaporators 4.
Running water produces high-temperature steam through steam generator (S101) 11, starts as system and is dropped with raw steam into two effects
Film evaporator 4, is inhaled into after Roots's vapour compression machine 6, increasing temperature and pressure by gas-liquid separator 5 and enters an effect falling film evaporator 9,
Circulated along steam-return line, until pressure reaches setting state in an effect falling film evaporator 9, close running water water intaking valve QV07 and
Steam generator (S101) 11 is switched, and system enters the normal evaporative crystallization stage.
Comparative example 1
Reference implementation example 1, difference is.
The Nacl waste water that the industries such as chemical industry, food are produced, mass concentration is 5%, uses conventional single stage MVR evaporative crystallizations
Method, 88 DEG C are heated to by raw material, and material liquid is directly mixed with concentrate to be become after saturated solution, into an effect falling film evaporator
Be evaporated crystallization in (an effect falling film evaporator pressure is 70.1Kpa), the elevation of boiling point of this evaporation process solution influence because
Element is clearly present always.
Traditional waste water evaporation and crystal process, turns into after the brine waste of 5% concentration is directly mixed with supersaturated feed liquid
Saturation feed liquid, then passes to 6 DEG C of the boiling point liter that falling film evaporator is evaporated material solution under crystallization, this method evaporation process
~8 DEG C, and the theoretical heat exchange amount Q=m*h*A* Δ t in evaporation process, m, h, A, Δ t is respectively quality of material, evaporator heat exchange
The mean temperature difference of area, evaporating heat exchanger heat transfer coefficient, heated side and heat side.When solution boiling point liter is clearly present, evaporation
During actual heat exchange amount Q1=m*h*A* (Δ t-8), MVR the system heat transfer temperature difference are smaller, take t=20 DEG C of Δ；And use this hair
Method described in bright, first carries out low concentration material evaporation process, then carries out saturation feed liquid crystallization process, can effectively reduce highly concentrated
Spend brine waste evaporation and crystal process mid-boiling point and rise influence to evaporation process evaporation intensity, now actual heat exchange amount can approximate table
It is shown as Q2Heat exchange amount improves about 30% in=0.5*m*h*A* Δ t+0.5*m*h*A* (Δ t-8), evaporator, and evaporation intensity is also big
Amplitude is improved.
The effect of single-stage two evaporative crystallisation process of the present invention is divided into low concentration for high salt concentration water evaporation crystallization process
Evaporation process and supersaturated crystallization process, can improve efficiency of energy utilization and overall evaporation efficiency with cascade utilization high-temperature steam.
Explanation above is only intended to help and understands technical scheme and its core concept, it is noted that for
For those skilled in the art, under the premise without departing from the principles of the invention, some change can also be carried out to the present invention
Enter and modify, these are improved and modification is also fallen into the protection domain of the claims in the present invention.
Claims (9)
1. a kind of evaporative crystallisation process for being used to handle brine waste, it is characterised in that comprise the following steps：
(1) brine waste is passed sequentially through after electromagnetic wave launcher and one-level preheater, brine waste is preheated to less than two
1 DEG C~3 DEG C of the corresponding saturation temperature of pressure in falling film evaporator are imitated, is passed through in two effect falling film evaporators and is evaporated concentration,
The material of the process is in unsaturated state, will be passed through gas-liquid separation by a concentrate after two effect falling film evaporator evaporations
Device is separated, and after gas-liquid separator separates a concentrate is heated to less than an effect falling film evaporation by material reheater
1 DEG C of the corresponding saturation temperature of pressure in device~3 DEG C, is passed through in an effect falling film evaporator and is evaporated crystallization, and falling liquid film is imitated one
The secondary concentration liquid obtained in evaporator after evaporative crystallization is in hypersaturated state, and supersaturated solution boiling point now is higher than an effect
The boiling point of the aqueous solution under falling film evaporator corresponding pressure；Secondary concentration liquid is passed through crystal separator Crystallization Separation, crystallization point
The concentrated solution of the saturation state obtained from device is passed through in an effect falling film evaporator and is evaporated again, the crystalline substance that crystal separator is obtained
Body is discharged by solid discharge device；
(2) brine waste enters an effect falling film evaporator after two effect falling film evaporators are concentrated by evaporation, two effect falling film evaporators
Steam of the concentrate after gas-liquid separator separates is boosted by vapour compression machine, is passed through after being boosted through vapour compression machine
One effect falling film evaporator is as the thermal source of an effect falling film evaporator, the secondary concentration liquid obtained after an interior evaporation of effect falling film evaporator
The steam obtained in crystallized separator, process is evaporated as the thermal source of two effect falling film evaporators.
2. the evaporative crystallisation process according to claim 1 for being used to handle brine waste, it is characterised in that：In step (1)
Brine waste is passed sequentially through after electromagnetic wave launcher, one-level preheater and two grades of preheaters, two effect falling film evaporators are passed through
Interior evaporation, enters back into crystallization in an effect falling film evaporator.
3. the evaporative crystallisation process according to claim 1 or 2 for being used to handle brine waste, it is characterised in that：Described
The condensed water that steam in one effect falling film evaporator is produced after being heated as thermal source discharges a part of heat by material reheater
Amount, then by one-level preheater absorb heat after, condensed water is discharged.
4. the evaporative crystallisation process according to claim 1 or 2 for being used to handle brine waste, it is characterised in that：Described
The condensed water that steam in two effect falling film evaporators is produced after being heated as thermal source is expelled directly out, or the condensed water enters two grades
After preheater heat absorption, then the condensed water discharged.
5. a kind of device for being used to handle the evaporative crystallisation process of brine waste realized described in claim 1, it is characterised in that：
Including electromagnetic wave launcher, one-level preheater, two grades of preheaters, two effect falling film evaporators, gas-liquid separator, material reheating
Device, an effect falling film evaporator and crystal separator, one-level preheater are connected with first material transfer pipeline, described electromagnetic wave hair
Injection device is arranged on first material transfer pipeline, and described one-level preheater and two grades of preheaters pass through second material delivery pipe
Road is connected, and described one-level preheater and two effect falling film evaporators are connected by 3 material transfer pipeline, the second described thing
Material conveying tube road and 3 material transfer pipeline are connected in parallel, and two described effect falling film evaporators and gas-liquid separator pass through the 4th
Material delivery pipe road is connected, and described gas-liquid separator is connected with material reheater by the 5th material delivery pipe road, described
Material reheater and an effect falling film evaporator are connected by the 6th material delivery pipe road, a described effect falling film evaporator and crystallization
Separator is connected by the 7th material delivery pipe road；A described effect falling film evaporator bottom is provided with first material outlet, one
Primary concentration liquid in effect falling film evaporator is delivered to through first material outlet by the 8th material delivery pipe road is arranged at an effect
First material entrance at the top of falling film evaporator, makes primary concentration liquid be crystallized in an effect falling film evaporator, two described effect drops
The brine wastes that film evaporator bottom is provided with second material outlet, two effect falling film evaporators pass through the through second material outlet
Nine material delivery pipe roads are delivered to the second material entrance being arranged at the top of two effect falling film evaporators, make brine waste in two effect drops
Evaporated in film evaporator；The first steam (vapor) outlet is provided with the top of gas-liquid separator, the steam in gas-liquid separator is passed through first
Steam pipework is delivered to vapour compression machine, steam is increased to the temperature and pressure specified, then convey by the second steam pipework
To an effect falling film evaporator as thermal source, crystal separator top is provided with the second steam (vapor) outlet, by the steaming in crystal separator
Vapour is delivered to the first steam inlet being arranged on the outside of two described effect falling film evaporators by the 3rd steam pipework.
6. the device according to claim 5 for realizing the evaporative crystallisation process for handling brine waste, it is characterised in that：
First condensation-water drain of described effect falling film evaporator passes through the with described material reheater and one-level preheater successively
One condensate line and the connection of the second condensate line, the second condensation-water drain and water tank of described two effects falling film evaporators
Condensing water inlet connected by the 4th condensate line, the 3rd condensation-water drain of described water tank and two grades of preheaters lead to
Cross the connection of the 5th condensate line, the second condensation-water drain of described two effects falling film evaporators by the 3rd condensate line with
Condensate drain outlet is connected, and the 3rd described condensate line and the 4th described condensate line are connected in parallel.
7. the device according to claim 5 for realizing the evaporative crystallisation process for handling brine waste, it is characterised in that：
The second regulating valve and the of regulation mass flow is provided with described second material transfer pipeline and 3 material transfer pipeline
Matter Transfer pump is provided with three regulating valves, the 8th described material delivery pipe road and the 9th material delivery pipe road.
8. the device according to claim 5 for realizing the evaporative crystallisation process for handling brine waste, it is characterised in that：
The 4th regulating valve of regulation steam flow is provided with the 4th described steam pipework.
9. the device according to claim 5 for realizing the evaporative crystallisation process for handling brine waste, it is characterised in that：
Described electromagnetic wave launcher is high-frequency electromagnetic wave launcher, and described vapour compression machine is Roots's vapour compression machine.
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| CN108031132A (en) * | 2018-01-12 | 2018-05-15 | 无锡宝南机器制造有限公司 | Double tower falling film evaporator group |
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| CN114887340A (en) * | 2022-04-29 | 2022-08-12 | 江苏才信通科技有限公司 | Double-effect MVR forced countercurrent circulation falling film evaporation crystallization system |
| CN114887340B (en) * | 2022-04-29 | 2024-04-09 | 江苏才信通科技有限公司 | Double-effect MVR forced countercurrent circulation falling film evaporation crystallization system |
| CN115583768A (en) * | 2022-10-20 | 2023-01-10 | 江苏远方动力科技有限公司 | High-ore desalted water evaporation crystallization device and high-ore desalted water treatment method |
| CN116062775B (en) * | 2023-02-17 | 2024-06-04 | 中国天辰工程有限公司 | Ammonium sulfate evaporation crystallization process and system |
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Application publication date: 20170718 |