CN208603749U - A kind of sodium chloride ammonium chloride divides salt device - Google Patents
A kind of sodium chloride ammonium chloride divides salt device Download PDFInfo
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- CN208603749U CN208603749U CN201820786215.4U CN201820786215U CN208603749U CN 208603749 U CN208603749 U CN 208603749U CN 201820786215 U CN201820786215 U CN 201820786215U CN 208603749 U CN208603749 U CN 208603749U
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Abstract
The utility model discloses a kind of sodium chloride ammonium chlorides to divide salt device, system is precipitated including sequentially connected pre-heating system, sodium chloride crystal and system is precipitated in ammonia chloride crystal, and the vapour compression machine of system and ammonia chloride crystal precipitation system progress heat exchange is precipitated with sodium chloride crystal respectively.Sodium chloride is crystallized be precipitated at high operating temperatures by the utility model, oversaturated ammonium chloride is precipitated under low-temperature condition, to realize the separation and recycling of sodium chloride in waste water, ammonium chloride, the sodium chloride and ammonium chloride product of technical grade are obtained, reduce the generation of solid waste or dangerous waste, without the emission for causing river pollution, the technical effect of the resource reclaim of no pollution liquid discharge is reached.
Description
Technical field
The utility model relates to field of environment protection equipment, and in particular to a kind of sodium chloride ammonium chloride divides salt device.
Background technique
Waste water is the general name of the water being discharged in people's active procedure and runoff rainwater, generally comprises sanitary sewage, industry
Waste water and diameter flow into the other useless water of rainwater grade of drainpipe, belong to one of big public hazards of orchid of nature, wherein industrial wastewater is
The waste water and waste liquid generated in the industrial production contains industrial production materials, intermediate product, byproduct and the life outflowed with water
The pollutant generated during producing, with the rapid development of industry, the type and quantity of waste water rapidly increase, the pollution to water body
Also increasingly extensively and serious, the health and safety of the mankind is threaten, while also containing a large amount of recoverable resources in sewage, such as
It is not recycled, will bring about great losses, therefore sewage is developed and comprehensively utilized, turning harm into good is particularly important.
Metallurgical Waste Water, chemical waste water main component are substantially inorganic salts and all kinds of mixed salts, in production as industry is raw
Produce device continuous construction, sewage, exhaust gas, waste discharge amount be also continuously increased, however the whole world environmental issue increasingly
Seriously, the continuous increase of environmentally friendly dynamics, so resource recovery process is also constantly being promoted.Currently, although each enterprise is actively equipped with
Evaporated crystallization device handles high-salt wastewater, but still remains many problems.The technique that enterprise uses at present is to have recycled absolutely mostly
Most water has simultaneously obtained crystal salt, but since obtained crystal salt is carnallite, it not only cannot be by resource utilization instead
Understand according to the qualitative disposition of dangerous waste, meanwhile, liquid waste processing is not thorough, and still there are a large amount of separating liquids to need to discharge, and discharging of waste liquid is still
It can cause river pollution, treatment process energy consumption is high, and these problems annoying enterprise, and have seriously affected the project process of enterprise,
Zero liquid of high-salt wastewater discharges and recycling treatment is the inexorable trend that high-salt wastewater is administered.
Mixed salt is formed after existing sodium chloride ammonium chloride evaporation, dangerous waste processing can only be done, Nacl cannot be done.Dangerous waste processing
It needs to spend a large amount of disposal costs, and Nacl can produce economic benefit.
Utility model content
In order to solve the above technical problems, we have proposed a kind of sodium chloride ammonium chlorides to divide salt device, solves the prior art
Middle carnallite forms solid waste, causes environmental pollution, reaches the mesh for reducing pollution, improving water reuse rate, reducing fixed-end forces cost
's.
In order to achieve the above objectives, the technical solution of the utility model is as follows:
A kind of sodium chloride ammonium chloride divides salt device, including sequentially connected pre-heating system, sodium chloride crystal be precipitated system and
System is precipitated in ammonia chloride crystal, and system and ammonia chloride crystal precipitation system progress heat exchange is precipitated with sodium chloride crystal respectively
Vapour compression machine.
Further, the pre-heating system includes raw material surge tank, feed pump, hot water preheater, vapor preheater, condensation
Water pump and condensate water pot, wherein the raw material surge tank, the feed pump, the hot water preheater and the vapor preheater
It is sequentially connected with, system and the chlorination is precipitated from vapor preheater, the sodium chloride crystal for receiving in the condensate water pot
The condensed water of system is precipitated in ammonium crystal, and the condensate pump is used to for the condensed water in the condensate water pot to be delivered to hot water preheating
Device is as heat source.
Further, it includes primary heater, primary cycle pump, level-one separation that system, which is precipitated, in the sodium chloride crystal
Device, level-one discharging pump, level-one thickener, first-stage centrifugal machine, primary mother liquor tank and level-one discharging pump, the side of the primary separator
Wall is successively arranged first charging aperture, second charging aperture, third feed inlet and the 4th feed inlet, the first charging aperture from top to bottom
For receiving the waste liquid that system is precipitated from the ammonia chloride crystal；The charging of the third feed inlet and the primary heater
Primary cycle pipe is equipped between mouthful；
The waste liquid preheated through the vapor preheater is delivered to the primary cycle pipe, and wherein gas phase enters a fraction
From in device, liquid phase enters in the primary heater；Material in the primary heater passes through primary cycle pump conveying
To the second charging aperture；The level-one discharging pump is used to the material of the primary separator being delivered to the level-one thickener
In；
The first-stage centrifugal machine is used to for the material in the level-one thickener being separated by solid-liquid separation, and it is female that liquid enters the level-one
Flow container is pumped into the ammonia chloride crystal through the level-one discharging pump and system is precipitated.
Further, the feed end of the discharge end of the primary separator and the level-one thickener flows back equipped with level-one
Pipe, Partial Liquid Phase turns when being delivered to the level-one thickener through the level-one discharging pump convenient for the liquid phase in the primary separator
Gas phase is turned to, gas phase just enters in the primary separator from the level-one return pipe；
Further, it includes secondary heater, secondary cycle pump, the second-order separation that system, which is precipitated, in the ammonia chloride crystal
Device, second level discharging pump, second level thickener, two-stage centrifugal machine, secondary mother liquor tank and second level discharging pump, the side of the second-stage separator
Wall is successively arranged feed inlet one, feed inlet two and feed inlet three from top to bottom, the feed inlet two and the secondary heater
Secondary cycle pipe is equipped between feed inlet；
Waste liquid is pumped into the secondary cycle pipe by the level-one discharging pump, and wherein gas phase enters in the second-stage separator,
Liquid phase enters in the secondary heater；Material in the secondary heater by secondary cycle pump be delivered to it is described into
Material mouth one；Material in the second-stage separator is delivered in the second level thickener through the second level discharging pump；
The two-stage centrifugal machine is used to for the material in the second level thickener being separated by solid-liquid separation, and it is female that liquid enters the second level
Flow container is pumped into the primary separator through the first charging aperture through the second level discharging pump and continues circulating and evaporating concentration.
Further, the feed end of the discharge end of the second-stage separator and the second level thickener flows back equipped with second level
Pipe, Partial Liquid Phase turns when being delivered to the second level thickener through the second level discharging pump convenient for the liquid phase in the second-stage separator
Gas phase is turned to, gas phase just enters in second-stage separator from the second level return pipe.
Further, the second level thickener is equipped with the cold source that can cool down.
The technical solution of the utility model has the advantage that compared with prior art
Sodium chloride is crystallized be precipitated at high operating temperatures by the utility model, analyses oversaturated ammonium chloride under low-temperature condition
Out, to realize the separation and recycling of sodium chloride in waste water, ammonium chloride, the sodium chloride and ammonium chloride for having obtained technical grade are produced
Product, reduce the generation of solid waste or dangerous waste, and no emission for causing river pollution has reached the resource reclaim of no pollution liquid discharge
Technical effect.
The utility model device is simple, it is easy to accomplish, high degree of automation, operating cost is low, meets sustainable development and wants
It asks, can be widely applied to during actual industrial production.
Detailed description of the invention
In order to illustrate the embodiment of the utility model or the technical proposal in the existing technology more clearly, below will be to embodiment
Or attached drawing needed to be used in the description of the prior art is briefly described, it should be apparent that, the accompanying drawings in the following description is only
It is some embodiments of the utility model, for those of ordinary skill in the art, in the premise not made the creative labor
Under, it is also possible to obtain other drawings based on these drawings.
Fig. 1 divides the signal of the equipment of salt crystallization processes for a kind of sodium chloride ammonium chloride disclosed in the utility model embodiment
Figure.
Number and corresponding component title represented by letter in figure:
1. 2. 4. condensate pump of feed pump 3-1. hot water preheater 3-2. vapor preheater of raw material surge tank, 5. level-one
6. primary cycle of heater pumps 7. primary separator 7-1. primary cycle pipe 7-2 level-one return pipe, 8. level-one discharging pump
9. 11. primary mother liquor tank of level-one thickener 9-1 level-one 10. first-stage centrifugal machine of bursting tube, 12. primary mother liquor pumps 13. second levels
14 secondary cycle of heater pumps the discharging of 15. second-stage separator 15-1 secondary cycle pipe 15-2 second level return pipe, 16. second level
Pump 17. 19. secondary mother liquor tank of second level thickener 17-1 secondary safety 18. two-stage centrifugal machine of pipe, 20. secondary mother liquor pump 21.
22. condensate water pot a. cooling water inlet b. cooling water outlet of vapour compression machine
Specific embodiment
The following will be combined with the drawings in the embodiments of the present invention, carries out the technical scheme in the embodiment of the utility model
Clearly and completely describe, it is clear that the described embodiments are only a part of the embodiments of the utility model, rather than whole
Embodiment.Based on the embodiments of the present invention, those of ordinary skill in the art are without creative efforts
Every other embodiment obtained, fall within the protection scope of the utility model.
The utility model is described in further detail below with reference to embodiment and specific embodiment.
Embodiment 1
Such as Fig. 1, a kind of sodium chloride ammonium chloride divides salt device comprising sequentially connected pre-heating system, sodium chloride crystal analysis
System is precipitated in system and ammonia chloride crystal out, and be precipitated with sodium chloride crystal system respectively and ammonia chloride crystal be precipitated system into
The vapour compression machine of row heat exchange.
Pre-heating system includes raw material surge tank 1, feed pump 2, hot water preheater 3-1, vapor preheater 3-2, condensate pump 4
And condensate water pot 22, wherein raw material surge tank 1, feed pump 2, hot water preheater 3-1 and vapor preheater 3-2 are sequentially connected with,
Condensate water pot 22, which is used to receive, is precipitated system from vapor preheater 3-2 and sodium chloride crystal precipitation system and ammonia chloride crystal
Condensed water, condensate pump 4 are used to the condensed water in condensate water pot 22 being delivered to hot water preheater 3-1 as heat source；
It includes primary heater 5, primary cycle pump 6, primary separator 7, level-one discharging pump that system, which is precipitated, in sodium chloride crystal
8, level-one thickener 9, first-stage centrifugal machine 10, primary mother liquor tank 11 and level-one discharging pump 12, primary heater 5 and level-one separation
Device 7 is vertically arranged, and the top of primary heater 5 is feed inlet, and bottom end is discharge port；The top of primary separator 7 is gas
It mutually exports, bottom end is discharge port, and the side wall of primary separator 7 is successively arranged first charging aperture, second charging aperture, the from top to bottom
Three feed inlets and the 4th feed inlet, first charging aperture are used to receive the waste liquid that system is precipitated from ammonia chloride crystal；Third charging
Circulation pipe 7-1 is equipped between mouth and the feed inlet of primary heater；
The waste liquid preheated through vapor preheater 3-2 is delivered to circulation pipe 7-1, and wherein gas phase enters in primary separator 7, liquid
Mutually enter in primary heater 5；Material in primary heater 5 is delivered to second charging aperture by primary cycle pump 6；Level-one goes out
Material pump 8 is for the material of primary separator 7 to be delivered in level-one thickener 9；The discharge end and level-one stiff of primary separator 7
The feed end of device 9 is equipped with level-one return pipe 7-2, and it is thick through level-one discharging pump 8 to be delivered to level-one convenient for the liquid phase in primary separator 7
Partial Liquid Phase is converted into gas phase when thick device 9, and gas phase just enters in primary separator 7 from level-one return pipe 7-2；
For first-stage centrifugal machine 10 for the material in level-one thickener 9 to be centrifugated out, mother liquor enters primary mother liquor tank
11, ammonia chloride crystal is pumped into through level-one discharging pump 12, and system is precipitated.
It includes secondary heater 13, secondary cycle pump 14, second-stage separator 15, second level that system, which is precipitated, in the ammonia chloride crystal
Discharging pump 16, second level thickener 17, two-stage centrifugal machine 18, secondary mother liquor tank 19 and second level discharging pump 20,13 He of secondary heater
Second-stage separator 15 is vertically arranged, and the top of secondary heater 13 is feed inlet, and bottom end is discharge port；Second-stage separator 15
Top be gaseous phase outlet, bottom end is discharge port, and the side wall of second-stage separator 15 is successively arranged feed inlet one, charging from top to bottom
Mouth two and feed inlet three are equipped with circulation pipe 15-1 between feed inlet two and the feed inlet of secondary heater 13；
Waste liquid is pumped into circulation pipe 15-1 by level-one discharging pump 12, and wherein gas phase enters in second-stage separator 15, and liquid phase enters
In secondary heater 13；Material in secondary heater 13 is delivered to feed inlet one by secondary cycle pump 14；Second-stage separator
Material in 15 is delivered in second level thickener 17 through second level discharging pump 16；The discharge end of second-stage separator and second level thickener
Feed end is equipped with second level return pipe 15-2, when being delivered to second level thickener through second level discharging pump convenient for the liquid phase in second-stage separator
Partial Liquid Phase is converted into gas phase, and gas phase just enters in second-stage separator from the second level return pipe；
For two-stage centrifugal machine for the material in second level thickener to be centrifugated out, mother liquor enters secondary mother liquor tank, warp
Second level discharging pump is pumped into primary separator 7 through first charging aperture continues circulating and evaporating concentration.
Wherein, second level thickener 17 be equipped with cooling water inlet a and cooling water outlet b, for be passed through low-temperature cooling water or its
The media such as its refrigerated brine cool down property.
A kind of sodium chloride ammonium chloride divides salt crystallization processes, and sodium chloride mass fraction is 6.08% in waste water, ammonium chloride quality
Score is 5.35%, and the total flow of waste water is 10.8t/h, is included the following steps:
S1. it preheats, waste water squeezes into preheater by feed pump 2 by raw material surge tank 1 and tentatively heated up, and heating is divided into two
Step: waste water first passes through hot water preheater (hot water plate type preheater) 3-1 heating, and the high-temperature condensation water that heat source is 105 DEG C gives up
Liquid can be heated to 82 DEG C；It is heated using vapor preheater (i.e. steam-plate type preheater) 3-2, the steam that this heat source is 110 DEG C,
Waste water can be heated to 93-95 DEG C；
S2. it is concentrated by evaporation and obtains oversaturated sodium chloride waste water, the waste water after preheating in step S1 is via primary separator 7
Primary cycle pipe 7-1 enter primary heater 5 and carry out heat exchange heating, the waste liquid after heating is delivered to one through primary cycle pump 6
In grade separator 7, waste liquid interior progress gas-liquid separation (about 85 DEG C of gas phase temperature, about 94 DEG C of liquidus temperature) in primary separator 7,
Evaporation and concentration makes the sodium chloride of liquid phase reach supersaturation, and (ammonium chloride unsaturated solution at this time controls sodium chloride concentration >
28.5%, ammonium chloride concentration < 35%) when, by level-one discharging pump 8, squeeze into level-one thickener 9, at the same time, gas phase into
Enter vapour compression machine 21 to recompress, 85 DEG C, 105 DEG C of outlet temperature of 21 inlet temperature of vapour compression machine；
S3. Isolating chlorinated sodium, level-one thickener 9 is to oversaturated sodium chloride waste water (sodium chloride concentration > obtained in S2
28.5%, ammonium chloride concentration < 35%) further first-stage centrifugal machine 10 is squeezed into after thickening, sodium chloride crystal passes through first-stage centrifugal machine
10 are centrifuged out, and the sodium chloride liquid of low concentration enters primary mother liquor tank 11 as primary mother liquor；
S4. it is concentrated by evaporation and obtains oversaturated ammonium chloride waste-water, it will be in primary mother liquor tank 11 by primary mother liquor pump 12
Primary mother liquor squeezes into the secondary cycle pipe 15-1 of second-stage separator 15, enters two by the secondary cycle pipe 15-1 of second-stage separator 15
Grade heater 13, carries out heat exchange heating (temperature is heated to 100 DEG C or so), and the waste liquid after heating is through 14 conveying of secondary cycle pump
Into second-stage separator 15, waste liquid carries out gas-liquid separation in second-stage separator 15, and about 85 DEG C of gas phase temperature, liquidus temperature is about
100 DEG C, when evaporation and concentration makes the ammonium chloride of liquid phase reach supersaturation (ammonium chloride concentration > 35% is controlled 45% or so), lead to
Second level discharging pump 16 is crossed, second level thickener 17 is squeezed into, gas phase enters the recompression of vapour compression machine 21；Vapour compression machine inlet temperature
85 DEG C, 105 DEG C of outlet temperature；
S5. separating ammonium chloride, second level thickener 17 are cooled to by circulating water cooling to continuing through chilled water after 40 DEG C
25 DEG C, liquid squeezes into two-stage centrifugal machine 18 after further thickening, and ammonia chloride crystal is centrifuged out by two-stage centrifugal machine 18, mother liquor
Become secondary mother liquor into secondary mother liquor tank 19.
S6. Recycling Mother Solution, the secondary mother liquor (9.8% sodium chloride, 18.2% ammonium chloride) after S5 is separated pass through two
Grade mother liquor pumps 20 reuses into the primary separator 7 of step S2, is evaporated concentration again.
Further, the feed end of the discharge end of primary separator 7 and level-one thickener 9 is equipped with level-one return pipe 7-2,
Partial Liquid Phase is converted into gas phase, gas when being delivered to level-one thickener 9 through level-one discharging pump 8 convenient for the liquid phase in primary separator 7
Mutually just enter in primary separator 7 from level-one return pipe 7-2.The setting of level-one return pipe 7-2 is not only convenient for returning for gas phase
Stream, and be conducive to the safety of lifting means, maintain the pressure balance of level-one thickener and whole system.
Further, the level-one bursting tube for gas-liquid equilibrium is connected between level-one thickener 9 and primary mother liquor tank 11
9-1 can be obviously improved the safety of system.
Likewise, the discharge end of second-stage separator 15 and the feed end of second level thickener 17 are equipped with second level return pipe 15-1,
Partial Liquid Phase is converted into gas phase, gas when being delivered to second level thickener 17 through second level discharging pump convenient for the liquid phase in second-stage separator 15
Mutually just enter in second-stage separator 15 from second level return pipe 15-1.The setting of second level return pipe is not only convenient for the reflux of gas phase,
And be conducive to the safety of lifting means, maintain the pressure balance of second level thickener and whole system.
Primary heater 5 and secondary heater 13 exchange heat after high-temperature condensation water (about 95 DEG C) and vapor preheater 3-2
Hot water (about 105 DEG C of steam condensate (SC), specifically by vapor (steam) temperature depending on) is condensed, into condensate water pot 22, in condensate water pot 22
High-temperature condensation water heat source of the hot water preheater 3-1 as preheater is squeezed by condensate pump 4, the condensed water after heat exchange is (about
40 DEG C) go out battery limit (BL).
In this example, hot water plate type preheater 3-1 is using (heat exchange area: 50m2, single process, plate thickness 0.6mm；Plate
Material TA2, gasket material EPDM), heat source is the time condensation liquid of forced-circulation evaporator (which refers to), steam-plate type preheating
Device 3-2 is using (heat exchange area: 15m2, single process, plate thickness 0.6mm；Plate material TA2, gasket material EPDM), heat source is
105~115 DEG C of steam, flow are about 350kg/h.
Table 1
It can be seen that from upper table, after this technique high salinity wastewater treatment, sodium chloride, the sodium chloride rate of recovery are high, thus
So that low energy consumption.
Embodiment 2
As shown in Figure 1, device structure in this example, with embodiment 1, this will not be repeated here.
A kind of sodium chloride ammonium chloride divides salt crystallization processes, and sodium chloride mass fraction is 5.53% in waste water, ammonium chloride quality
Score is 7.02%, and the total flow of waste water is 24.78t/h, is included the following steps:
S1. it preheats, waste water squeezes into preheater by feed pump 2 by raw material surge tank 1 and tentatively heated up, and heating is divided into two
Step: waste water first passes through hot water preheater (hot water plate type preheater) 3-1 heating, and the high-temperature condensation water that heat source is 105 DEG C gives up
Liquid can be heated to 81 DEG C；It is heated using vapor preheater (i.e. steam-plate type preheater) 3-2, the steam that this heat source is 110 DEG C,
Waste water can be heated to 95 DEG C；
S2. it is concentrated by evaporation and obtains oversaturated sodium chloride waste water, the waste water after preheating in step S1 is via primary separator 7
Circulation pipe 7-1 enter primary heater 5 and carry out heat exchange heating, the waste liquid after heating is delivered to a fraction through primary cycle pump 6
From in device 7, waste liquid interior progress gas-liquid separation (about 85 DEG C of gas phase temperature, about 94 DEG C of liquidus temperature) in primary separator 7 is evaporated
Concentration makes the sodium chloride of liquid phase reach supersaturation, and (ammonium chloride unsaturated solution at this time controls sodium chloride concentration > 28.5%, chlorine
Change ammonium concentration < 35%) when, it by level-one discharging pump 8, squeezes into level-one thickener 9, at the same time, gas phase enters both vapor compression
Machine 21 recompresses, and 85 DEG C, 105 DEG C of outlet temperature of 21 inlet temperature of vapour compression machine；
S3. Isolating chlorinated sodium, level-one thickener 9 is to oversaturated sodium chloride waste water (sodium chloride concentration > obtained in S2
28.5%, ammonium chloride concentration < 35%) further first-stage centrifugal machine 10 is squeezed into after thickening, sodium chloride crystal passes through first-stage centrifugal machine
10 are centrifuged out, and the sodium chloride liquid of low concentration enters primary mother liquor tank 11 as primary mother liquor；
S4. it is concentrated by evaporation and obtains oversaturated ammonium chloride waste-water, it will be in primary mother liquor tank 11 by primary mother liquor pump 12
Primary mother liquor squeezes into the secondary cycle pipe 15-1 of second-stage separator 15, enters two by the secondary cycle pipe 15-1 of second-stage separator 15
Grade heater 13, carries out heat exchange heating (temperature is heated to 100 DEG C or so), and the waste liquid after heating is through 14 conveying of secondary cycle pump
Into second-stage separator 15, waste liquid carries out gas-liquid separation in second-stage separator 15, and about 85 DEG C of gas phase temperature, liquidus temperature is about
100 DEG C, when evaporation and concentration makes the ammonium chloride of liquid phase reach supersaturation (ammonium chloride concentration > 35% is controlled 45% or so), lead to
Second level discharging pump 16 is crossed, second level thickener 17 is squeezed into, gas phase enters the recompression of vapour compression machine 21；Vapour compression machine inlet temperature
85 DEG C, 105 DEG C of outlet temperature；
S5. separating ammonium chloride, second level thickener 17 are cooled to by circulating water cooling to continuing through chilled water after 40 DEG C
25 DEG C, liquid squeezes into two-stage centrifugal machine 18 after further thickening, and ammonia chloride crystal is centrifuged out by two-stage centrifugal machine 18, mother liquor
Become secondary mother liquor into secondary mother liquor tank 19.
S6. Recycling Mother Solution, the secondary mother liquor (9.8% sodium chloride, 18.2% ammonium chloride) after S5 is separated pass through two
Grade mother liquor pumps 20 reuses into the primary separator 7 of step S2, is evaporated concentration again.
Primary heater 5 and secondary heater 13 exchange heat after high-temperature condensation water (about 95 DEG C) and vapor preheater 3-2
Hot water (about 105 DEG C of steam condensate (SC), specifically by vapor (steam) temperature depending on) is condensed, into condensate water pot 22, in condensate water pot 22
High-temperature condensation water heat source of the hot water preheater 3-1 as preheater is squeezed by condensate pump 4, the condensed water after heat exchange is (about
40 DEG C) go out battery limit (BL).
In this example, hot water plate type preheater is using (heat exchange area: 110m2, single process, plate thickness 0.6mm；Sheet
Matter TA2, gasket material EPDM), heat source be forced-circulation evaporator time condensation liquid, steam-plate type preheater using
(heat exchange area: 35m2, single process, plate thickness 0.6mm；Plate material TA2, gasket material EPDM), heat source is 105~115 DEG C
Steam, flow are about 800kg/h.
Table 2
It can be seen that from upper table, after this technique high salinity wastewater treatment, sodium chloride, the sodium chloride rate of recovery are high, thus
So that low energy consumption.
Above-described is only preferred embodiments of the present invention, it is noted that for the ordinary skill of this field
For personnel, without departing from the concept of the present invention, various modifications and improvements can be made, these all belong to
In the protection scope of the utility model.
Claims (7)
1. a kind of sodium chloride ammonium chloride divides salt device, which is characterized in that analysed including sequentially connected pre-heating system, sodium chloride crystal
System is precipitated in system and ammonia chloride crystal out, and be precipitated with sodium chloride crystal system respectively and ammonia chloride crystal be precipitated system into
The vapour compression machine of row heat exchange.
2. a kind of sodium chloride ammonium chloride according to claim 1 divides salt device, which is characterized in that the pre-heating system includes
Raw material surge tank, feed pump, hot water preheater, vapor preheater, condensate pump and condensate water pot, wherein the raw material buffering
Tank, the feed pump, the hot water preheater and the vapor preheater are sequentially connected with, and the condensate water pot comes from for receiving
System is precipitated in vapor preheater, the sodium chloride crystal and the condensed water of system, the condensed water is precipitated in the ammonia chloride crystal
Pump is for being delivered to hot water preheater as heat source for the condensed water in the condensate water pot.
3. a kind of sodium chloride ammonium chloride according to claim 2 divides salt device, which is characterized in that the sodium chloride crystal analysis
Out system include primary heater, primary cycle pump, primary separator, level-one discharging pump, level-one thickener, first-stage centrifugal machine,
Primary mother liquor tank and level-one discharging pump, the side wall of the primary separator be successively arranged from top to bottom first charging aperture, second into
System is precipitated from the ammonia chloride crystal for receiving in material mouth, third feed inlet and the 4th feed inlet, the first charging aperture
Waste liquid；Primary cycle pipe is equipped between the third feed inlet and the feed inlet of the primary heater；
The waste liquid preheated through the vapor preheater is delivered to the primary cycle pipe, and wherein gas phase enters the primary separator
In, liquid phase enters in the primary heater；Material in the primary heater is delivered to institute by primary cycle pump
State second charging aperture；The level-one discharging pump is for the material of the primary separator to be delivered in the level-one thickener；
The first-stage centrifugal machine is used to for the material in the level-one thickener being separated by solid-liquid separation, and liquid enters the primary mother liquor
Tank is pumped into the ammonia chloride crystal through the level-one discharging pump and system is precipitated.
4. a kind of sodium chloride ammonium chloride according to claim 3 divides salt device, which is characterized in that the primary separator
The feed end of discharge end and the level-one thickener is equipped with level-one return pipe, convenient for described in the liquid phase warp in the primary separator
Partial Liquid Phase is converted into gas phase when level-one discharging pump is delivered to the level-one thickener, and gas phase just enters from the level-one return pipe
In the primary separator.
5. a kind of sodium chloride ammonium chloride according to claim 4 divides salt device, which is characterized in that the ammonia chloride crystal analysis
Out system include secondary heater, secondary cycle pump, second-stage separator, second level discharging pump, second level thickener, two-stage centrifugal machine,
Secondary mother liquor tank and second level discharging pump, the side wall of the second-stage separator are successively arranged feed inlet one, feed inlet two from top to bottom
With feed inlet three, secondary cycle pipe is equipped between the feed inlet two and the feed inlet of the secondary heater；
Waste liquid is pumped into the secondary cycle pipe by the level-one discharging pump, and wherein gas phase enters in the second-stage separator, liquid phase
Into in the secondary heater；Material in the secondary heater is delivered to the feed inlet by secondary cycle pump
One；Material in the second-stage separator is delivered in the second level thickener through the second level discharging pump；
The two-stage centrifugal machine is used to for the material in the second level thickener being separated by solid-liquid separation, and liquid enters the secondary mother liquor
Tank is pumped into the primary separator through the first charging aperture through the second level discharging pump and continues circulating and evaporating concentration.
6. a kind of sodium chloride ammonium chloride according to claim 5 divides salt device, which is characterized in that the second-stage separator
The feed end of discharge end and the second level thickener is equipped with second level return pipe, convenient for described in the liquid phase warp in the second-stage separator
Partial Liquid Phase is converted into gas phase when second level discharging pump is delivered to the second level thickener, and gas phase just enters from the second level return pipe
In second-stage separator.
7. a kind of sodium chloride ammonium chloride according to claim 6 divides salt device, which is characterized in that the second level thickener is matched
Have the cold source that can cool down.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111302419A (en) * | 2020-01-06 | 2020-06-19 | 中伟新材料股份有限公司 | Process for solving problem of high evaporation boiling point of ammonia chloride by utilizing MVR |
| WO2023123365A1 (en) * | 2021-12-31 | 2023-07-06 | 东江环保股份有限公司 | System for determining end point of evaporation by means of image recognition during ammonia-nitrogen wastewater evaporative crystallization process |
| CN118005121A (en) * | 2024-01-25 | 2024-05-10 | 江苏赛德力制药机械制造有限公司 | Sodium carbonate and sodium bromide salt separating system and salt separating method |
-
2018
- 2018-05-24 CN CN201820786215.4U patent/CN208603749U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111302419A (en) * | 2020-01-06 | 2020-06-19 | 中伟新材料股份有限公司 | Process for solving problem of high evaporation boiling point of ammonia chloride by utilizing MVR |
| WO2023123365A1 (en) * | 2021-12-31 | 2023-07-06 | 东江环保股份有限公司 | System for determining end point of evaporation by means of image recognition during ammonia-nitrogen wastewater evaporative crystallization process |
| CN118005121A (en) * | 2024-01-25 | 2024-05-10 | 江苏赛德力制药机械制造有限公司 | Sodium carbonate and sodium bromide salt separating system and salt separating method |
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