CN205832669U - A kind of system of recovered material from crystallization feed liquid - Google Patents

Abstract

This utility model provides a kind of system of recovered material from crystallization feed liquid, and including the crystallization kettle being sequentially connected with, solid-liquid separating equipment, concentrator, the upper outlet of concentrator and lower part outlet are connected to the import of crystallization kettle.This utility model realizes recovery maximum to product, hence it is evident that reduces energy consumption, reduces environmental pollution simultaneously.The product quality that this utility model reclaims keeps consistent with outward appearance with certified products, and impurity content is low, is effectively improved yield and the purity of product, and then increases economic efficiency, it is achieved recovery maximum to product, hence it is evident that reduces energy consumption, alleviates environmental pollution simultaneously.

Description

A kind of system of recovered material from crystallization feed liquid

Technical field

This utility model belongs to material recovering system field, particularly relate to a kind of from crystallization feed liquid recovered material be System.

Background technology

During material production, crystallization feed liquid can be produced, containing portioned product in feed liquid, need to reclaim, different Recovery method, all there is significant difference in product quality and outward appearance that its response rate, cost recovery, recovery obtain.Some products Needing the measures such as heating when reclaiming, on the one hand to consume substantial amounts of heat energy, on the other hand, heat-sensitive substance, heating can make it Rotten or appearance color changes etc., affect product quality and outward appearance.For non-heat-sensitive material, setting used by existing recovery method Standby more, energy consumption is higher, and the response rate is low.

For heat-sensitive substance, as a example by aniline-acetonitrile, current recovery method is to be turned by aniline-acetonitrile reactant liquor Enter crystallization kettle, carry out cooling down with chuck and be simultaneously introduced a certain amount of production water and carry out sanding, when sanding liquid is cooled to necessarily After temperature, sanding liquid is put into centrifuge and is centrifuged isolated product, owing to mother solution at a temperature of this still having 1～2wt% Product, so needing to reclaim further, prior art is centrifuge mother liquor to be directly placed into one or more levels subsider sink Drop back to receive product, but caused by this product attribute, the product settled out can stick to settle on cell wall, it is impossible to directly reclaims, Squeeze into after crystallization kettle crystallizes again after needing when reclaiming product to be melted by product by steam or hot water and be centrifuged, both expended big Calorimetric amount and cold, belong to heat-sensitive substance due to nitriles substance again, misoperation when dissolving, and will result in portioned product polymerization Blackening, had both affected the main content of product, had caused again appearance poor.

Utility model content

The shortcoming of prior art in view of the above, the purpose of this utility model is that providing a kind of returns from crystallization feed liquid Receiving the system of material, for solving, the cost recovery of product in prior art is high, product recovery rate is low, product is rotten and appearance poor Etc. problem.

For achieving the above object and other relevant purposes, this utility model provides a kind of recovered material from the crystallization feed liquid System, including the crystallization kettle being sequentially connected with, solid-liquid separating equipment, concentrator, the upper outlet of described concentrator and lower part outlet It is connected to the import of crystallization kettle.On the one hand feed liquid is stirred by crystallization kettle, on the other hand, heats up feed liquid or drops Temperature, promotes that product separates out, and solid-liquid separating equipment carries out solid-liquid separation to feed liquid, reclaims and obtains solid product, and liquid divides from solid-liquid Flowing into concentrator from equipment, feed liquid is heated up or lowers the temperature by concentrator under agitation, promotes that product separates out, makes product exist Settling under action of gravity, lower floor forms dope, and upper strata forms clear liquid, and lower floor's dope is back to crystallization kettle to carry out repeating at recovery Reason, the supernatant is partly or entirely back to crystallization kettle and carries out repeating recycling.Heat up or cooling is according in crystallization feed liquid Depending on the characteristic of product, the product that the rising of solubility with temperature is raised, the feed liquid in crystallization kettle is carried out at cooling Reason so that product separates out from feed liquid, the product reduced for the rising of solubility with temperature, enters the feed liquid in crystallization kettle Row hyperthermic treatment so that product separates out from feed liquid.

Further, it is provided with waste liquid outlet between upper outlet and the crystallization kettle import of described concentrator.Concentrator upper strata The backflow volume of clear liquid determines than according to product, when the impact of Impurities Upon Product Quality is less, it is also possible to all reflux supernatant The products such as liquid, such as ammonium sulfate, carry out repeatedly circulation and stress, after processing end cycle, then using all of mother solution as waste liquid Discharge.When the impact of Impurities Upon Product Quality is bigger, it is also possible to all discharged as waste liquid by supernatant, no longer it is back to knot Brilliant still processes.

Further, the upper outlet of described concentrator connects clear liquid transfer tank.The upper liquid gone out from concentrator overflow After accumulating certain volume in clear liquid transfer tank, more partly or entirely proceed to crystallization kettle be carried out repeat recycling.

Further, it is provided with dope transfering material pump between lower part outlet and the crystallization kettle import of described concentrator, it is simple to by dense Lower floor's dope of close machine is quickly delivered to crystallization kettle.

Further, it is provided with clear liquid transfering material pump between upper outlet and the crystallization kettle import of described concentrator, it is simple to by dense The supernatant of close machine is quickly delivered to crystallization kettle.

Further, the number of units of described concentrator is one, two or multiple stage.The quantity of concentrator is according to the condition of production Fixed.

Further, the number of units of described concentrator is two or during multiple stage, the top of each concentrator is connected in series, respectively The lower part outlet of individual concentrator is connected to the import of crystallization kettle, it is achieved the overflow step by step of the supernatant, and then realizes repeatedly settling Separate, improve product recovery rate.

Further, described crystallization kettle is provided with production water inlet channel, when feed liquid is partly refluxed to crystallization kettle, passes through Produce water inlet channel and in crystallization kettle, supplement production water, to make up waste liquid output.

Further, described solid-liquid separating equipment is centrifuge, filter press, multi-functional pressure filter, suction filtration tank or pottery Porcelain filter.

As it has been described above, a kind of system of recovered material from crystallization feed liquid of the present utility model, have the advantages that For thermal sensitivity product, centrifuge mother liquor is carried out gravity settling separation, temperature control at stirring condition so that product no longer sticks to hold On wall, and after gravity settling separation, lower floor can obtain the dope that solid-to-liquid ratio is higher, by directly being squeezed into by this dope In crystallization kettle, blend with the feed liquid of normal batch, centrifugal recovery product, reclaim product by this system, it is entirely avoided steam Or the product polymerization defect that hot water material is brought, efficiently solve the product caused because of product polymerization in prior art and go bad, outward Seeing the problems such as difference, the product that this utility model reclaims by solid-liquid separating equipment isolated, does not has any rotten, outward appearance also with Normal product is consistent, hence it is evident that reduce substandard products accounting, improves product yield, obtains good economic benefit, also a saving simultaneously Heat and cold, save energy consumption, and, dense after supernatant part can be used for replacing producing water, reduce the outer discharge capacity of mother solution, And then alleviate the pollution to environment of the outer row's mother solution.For non-heat-sensitive product, this utility model also is able to be effectively improved product The response rate, reduces energy consumption, alleviates environmental pollution.

Accompanying drawing explanation

Fig. 1 is shown as recovery system structural representation of the present utility model.

Fig. 2 is shown as the cooling recovery system structural representation of this utility model embodiment 1.

Label declaration

1-crystallization kettle

2-solid-liquid separating equipment

3-concentrator

4-clear liquid transfer tank

5-dope transfering material pump

6-clear liquid transfering material pump

Detailed description of the invention

By particular specific embodiment, embodiment of the present utility model being described below, those skilled in the art can be by this Content disclosed by description understands other advantages of the present utility model and effect easily.

As it is shown in figure 1, recovery system of the present utility model, including the crystallization kettle 1 being sequentially connected with, solid-liquid separating equipment 2, dense Close machine 3, clear liquid transfer tank 4, the outlet of crystallization kettle 1 is connected to the import of solid-liquid separating equipment 2 by modes such as pipelines, and solid-liquid divides Be connected to the import of concentrator 3 by pipeline from the material liquid outlet of equipment 2, the lower part outlet of concentrator 3 is by dope conveying pipe Road and dope transfering material pump 5 are connected to the import of crystallization kettle 1, and the upper outlet of concentrator 3 is connected to clear liquid transfer by pipeline The import of tank 4, the outlet of clear liquid transfer tank 4 is connected to the import of crystallization kettle 1, clearly by clear liquid conveyance conduit, clear liquid transfering material pump 6 Liquid conveyance conduit is provided with waste liquid outlet, and for exclusive segment supernatant, crystallization kettle 1, concentrator 3 are provided with hydrophily coil pipe, root According to needs, feed liquid is heated or cooled.Cooling or the heating of concentrator 3 can use the shapes such as built-in coil pipe or external heat exchanger Formula realizes.Connection between above-mentioned each equipment is not limited to pipeline and connects, it is possible to realize the conveying of feed liquid.Work as feed velocity Time bigger, it is also possible to be not provided with clear liquid transfer tank 4 and carry out transfer accumulation, feed liquid is directly back to crystallization kettle 1 i.e. from concentrator 3 Can.The set-up mode of pump is not limited to the representation of Fig. 1 and Fig. 2, depending on the position according to each equipment, when needs are by feed liquid When low level is transported to a high position, then arranging water pump and carry out the conveying of feed liquid, certainly, horizontal feed can also arrange water pump, to add Fast transporting velocity.Such as, when the level height of crystallization kettle 1 is less than concentrator 3, the outlet of concentrator 3 and the import of crystallization kettle 1 Between pipeline on the most necessarily needing, dope transfering material pump 5 is set, clear liquid transfering material pump 6 carry out turn material, the supernatant of concentrator 3 Can be naturally downstream to crystallization kettle 1, now, the level height of solid-liquid separating equipment 2 can be higher than concentrator 3 and crystallization kettle 1, knot The feed liquid of brilliant still 1 outlet then needs to be delivered to solid-liquid separating equipment 2 by water pump, and the feed liquid of solid-liquid separating equipment 2 outlet is more certainly So downstream to concentrator 3, therefore, the setting of pump is can smooth delivery of power feed liquid be as the criterion.

After crystallization feed liquid enters crystallization kettle 1, the feed liquid in crystallization kettle 1 is in stirring, and stirring rod is at motor and subtracts Rotating under the drive of speed machine, PLC program controls the rotating speed of motor, it is achieved the control to feed liquid mixing speed, and crystallization kettle 1 sets There is production water water inlet pipe, produce and on water water inlet pipe, control valve is set, when needing to produce water, open control valve, can realize to knot Supplementing required production water in brilliant still 1, be full of hydrophily in the chuck of crystallization kettle 1, cold water or hot water in chuck are passed by chuck Heat, it is achieved cooling or the heating to feed liquid, the feed liquid in crystallization kettle 1 separates out crystal under cooling or with heating, containing crystal Feed liquid enter solid-liquid separating equipment 2 from crystallization kettle 1 by pipeline, solid-liquid separating equipment 2 makes solid product separate with liquid, Product flows out from solid outlet, it is achieved the recovery to solid product, and liquid then flows out from liquid outlet, is flowed into dense by pipeline Machine 3, the stirring rod in concentrator 3 carries out stirring at low speed to feed liquid, it is to avoid product is bonded in container inner wall, meanwhile, on concentrator 3 The rotation of Motor Control stirring rod so that feed liquid keep needed for mixing speed, concentrator 3 is provided with built-in coil pipe or Person's external heat exchanger, it is achieved feed liquid is heated or cooled, promotes that the product in feed liquid separates out, and the solid product of precipitation is at weight Settling downwards under power effect, therefore, lower floor is dope, and upper strata is clear liquid, and lower floor's dope flows out from bottom, by dope conveying pipe Road and dope transfering material pump 5 are back to crystallization kettle 1, it is achieved repeating to reclaim, the supernatant is flowed out in the way of overflow, passes through pipeline Enter clear liquid transfer tank 4, after the fluid accumulation in clear liquid transfer tank 4 to certain volume, by clear liquid conveyance conduit and clear liquid Transfering material pump 6, is partly refluxed to crystallization kettle 1, and another part is flowed out by the waste liquid outlet on clear liquid conveyance conduit, arranges as waste liquid Putting, waste liquid outlet is provided with control valve, controls fluid flow, and then controls liquid discharge capacity.Solid-liquid separating equipment 2 includes being centrifuged Machine, filter press, multi-functional pressure filter, suction filtration tank, ceramic filter etc., it is possible to realize solid-liquid separation.

The quantity of concentrator 3 could be arranged to one, two or multiple stage, when the quantity of concentrator 3 is two or during multiple stage, The bottom of each concentrator 3 is connected to crystallization kettle 1 by dope conveyance conduit and dope transfering material pump 5 so that lower floor's dope returns Flowing to crystallization kettle 1, contacted successively by pipeline in the top of each concentrator 3 so that clear liquid flows through each concentrator 3 step by step, real Now the most settlement separate, to improve the response rate of product to feed liquid.

Embodiment 1

The present embodiment is as a example by aniline-acetonitrile:

Aniline-acetonitrile belongs to dyestuff intermediate, is used for producing indigo, is slightly soluble in water, is soluble in ethanol, acetone, fusing point 40 ℃。

Fig. 2 is shown as the recovery system structural representation of the present embodiment.

The recovery method of a kind of aniline-acetonitrile product, comprises the following steps:

1), by aniline-acetonitrile sanding liquid proceed to, in crystallization kettle 1 (volume 15000L), be cooled to 30 DEG C, stirring of crystallization kettle 1 Mixing speed is 15r/min.In this step, the liquid volume in crystallization kettle 1 is relatively big, reaches 15000L, therefore, if be cooled to more Low temperature, can improve energy consumption, and then improves cost, is cooled to 30 DEG C, can make the product in sanding liquid can be from solution A large amount of precipitations.Being additionally provided with the inlet channel producing water on crystallization kettle 1, aniline-acetonitrile uses sanding crystallization, needs addition to produce Water carries out sanding to feed liquid, and the inflow producing water is the discharge capacity of waste liquid.

2), the mother solution of crystallization kettle 1 enters solid-liquid separating equipment 2, isolated product and mother solution by pipeline.

3) concentrator 3 (diameter 5m, highly 4.4m), by mother solution is proceeded to, by gravity settling separation feed liquid, in concentrator 3 Portion is provided with cooling water coil, and the feed liquid within concentrator 3 is cooled to 15 DEG C by cooling water coil, promotes the product knot in feed liquid Crystalline substance, the dope that concentrator 3 settles gained lower floor high solid-liquid ratio (product content 20～30wt%) is carried by dope transfering material pump 6 To crystallization kettle 1, mix with the material lowered the temperature in crystallization kettle 1, enter solid-liquid separating equipment 2 isolated product, centrifugal mother Liquid enters concentrator 3 and settles, circulation and stress.The mixing speed of concentrator 3 is 5r/min, the flow rate of liquid of entrance concentrator 3 is 25m³/h.The flow rate of liquid entering concentrator 3 is directly related with the treating capacity of crystallization kettle, and treating capacity is the biggest, and flow velocity is the biggest.Dense The supernatant overflow of machine 3 is to clear liquid transfer tank 4, after the fluid accumulation in clear liquid transfer tank 4 to certain volume, supernatant volume 60% is back to crystallization kettle 1, replaces part producing water to carry out sanding, and remaining clear liquid is discharged as waste liquid, enters waste water and processes After device carries out decontamination process, then drain in natural environment outward.The solid-liquid separating equipment 2 of the present embodiment is centrifuge.

The impact of product yield and product purity is tested by concentrator supernatant backflow volume

Containing partial salts material (generally about 0.5 weight %) from the supernatant that concentrator 3 overflow goes out, if Long-time this supernatant of reuse, can cause product quality to decline, and the backflow volume of concentrator supernatant is to from product yield and pure The impact such as following table of degree:

Table 1 concentrator supernatant backflow volume than with product purity statistical table

Wherein, concentrator supernatant backflow volume ratio refers to that the volume being back to crystallization kettle from the supernatant of concentrator accounts for The percentage ratio of the supernatant cumulative volume that concentrator flows out；Product yield=(contain in the product quality ÷ sanding liquid that recovery obtains Product quality) × 100%.As can be seen from Table 1, the supernatant gone out from concentrator 3 overflow, a part can only be back to knot Brilliant still 1 recycles, if being all back to crystallization kettle 1, product purity can be caused to decline, in turn result in quality and do not conform to Lattice.

The clean quality content of aniline-acetonitrile in the product that product purity i.e. reclaims.

The weight content statistical conditions such as following table of aniline-acetonitrile from the supernatant that concentrator 3 overflow goes out.Anilino-second The detection method of nitrile content includes chemical titration, liquid spectrum external standard method etc., and the present embodiment uses chemical titration.

The weight content statistical table of aniline-acetonitrile in the waste liquid that table 2 is got rid of

As can be seen from Table 2, in the waste liquid of eliminating, the weight content of aniline-acetonitrile as little as 0.5%, and keep permanent Fixed, it is achieved the efficient recovery to aniline-acetonitrile, increase economic efficiency.

The recovery method of aniline-acetonitrile in the present embodiment, uses concentrator to settle centrifuge mother liquor, lower the temperature, dense Liquid in machine is in the state being slowly stirred, it is ensured that product will not adhere on the wall, and through concentrator sedimentation point From rear, lower floor can obtain the dope that solid-to-liquid ratio is higher, is directly squeezed into by this dope in crystallization kettle and the sanding liquid of normal batch is mixed Mixed, centrifugal recovery product, reclaims product by the method, it is entirely avoided in prior art steam the product in subsider The product polymerization that vapour or hot water material are brought, and then solve the problems such as low, the appearance poor of product yield.

Table 3 product yield and visual condition statistical table

Product yield=(product quality contained in the product quality ÷ sanding liquid that recovery obtains) × 100%.

As can be seen from Table 3, the product yield that this utility model reclaims is apparently higher than existing steam or hot water material Method, and, the outward appearance of product that this utility model reclaims is faint yellow, for certified products, existing steam or hot water material method, due to Product having been carried out heat treated, has caused product heat damage, outward appearance is isabelline, and for substandard products, its price is significantly lower than this reality With the product of novel recovery, therefore, this utility model, on the premise of not affecting product appearance and quality, is effectively increased product Product yield, and then improve economic benefit.

Table 4 this utility model and prior art reclaim energy consumption and the discharging of waste liquid volume statistical table of product

As can be seen from Table 4, owing to this utility model need not steam or hot water material, therefore, saved heat and Cold, hence it is evident that reduce energy expenditure, dense after the supernatant be partly refluxed to crystallization kettle, play replace produce water effect, Reduce the consumption producing water, and reduce the outer discharge capacity of waste liquid, reduce the waste liquid pollution level to environment.

The recovery system of the present embodiment is as follows: crystallization kettle 1 is connected to solid-liquid separating equipment 2, and solid-liquid separating equipment 2 is connected to Concentrator 3, the bottom of concentrator 3 is connected to crystallization kettle 1 by dope conveyance conduit and dope transfering material pump 5, concentrator 3 upper Portion is connected to clear liquid transfer tank 4 by pipeline, and clear liquid transfer tank 4 is connected to by clear liquid conveyance conduit and clear liquid transfering material pump 6 Crystallization kettle 1, the clear liquid conveyance conduit between clear liquid transfer tank 4 and crystallization kettle 1 is provided with waste liquid outlet and flow control valve, stream Control valve controls the discharge capacity of waste liquid, and waste liquid outlet is connected to wastewater treatment equipment by pipeline, waste water outer row To natural environment.

Feed liquid is stirred by concentrator 3 one aspect, on the other hand, settlement separate to carrying out under cooling conditions, dense The bottom of machine 3 is all connected to crystallization kettle 1 by dope conveyance conduit, and the top of concentrator 3 is connected to clear liquid transfer by pipeline Tank, clear liquid is connected to crystallization kettle concentrator by conveyance conduit and feed liquid carries out dense sedimentation, stirring, dense while, the most right Feed liquid is heated or cooled, and to reduce product dissolubility in feed liquid, promotes that product separates out from feed liquid so that it is be settled down to Bottom concentrator, it is back to crystallization kettle by dope conveyance conduit and recycles, it is achieved recovery maximum to product.

Embodiment 2

The present embodiment is as a example by yellow sodium prussiate, and its recovery system is as in figure 2 it is shown, the yellow sodium prussiate product that separates through evaporation Material liquid enters crystallization kettle 1, and in crystallization kettle 1, the mixing speed of feed liquid is 40-70r/min, and the mixing speed of the present embodiment is 50r/min, slow cooling to 35 DEG C, enter solid-liquid separating equipment 2 and carry out solid-liquid separation, separating obtained mother solution enters concentrator 3 Carrying out settlement separate, in concentrator 3, the rotating speed of stirring rod is 3r/min, and in concentrator 3, feed liquid is cooled to 20 DEG C, concentrator 3 Lower floor's dope proceeds in crystallization kettle 1 by dope transfering material pump 5, mixes with normal batch crystallization feed liquid, enters back into solid-liquid separation and set Standby 2 are centrifuged, and the clear liquid of concentrator 3 upper strata overflow then enters clear liquid transfer tank 4, accumulate after certain volume, pass through clear liquid Transfering material pump 6 enters and repeats in crystallization kettle 1 to reclaim, and in the present embodiment, in clear liquid transfer tank 4, the clear liquid of 90% (volume ratio) is back to Crystallization kettle 1 is circulated recovery, and the clear liquid of 10% (volume ratio) is discharged as waste liquid.The solid-liquid separating equipment 2 of the present embodiment is Centrifuge.

The yellow sodium prussiate product yield that the present embodiment reclaims is 95%, and needed for often reclaiming 1 ton of product, energy consumption is that 12kg marks coal, In the waste liquid discharged, the content of yellow sodium prussiate is 2wt%, and reclaiming the product purity obtained is 98% (quality purity), reached with The similar technique effect of embodiment 1.In prior art, the recovery of yellow sodium prussiate is the mode using recycled mother solution, exists The whole Recycling Mother Solution set problems such as consumption is big, equipment needed thereby is many, energy consumption is high, drain in the mother solution of 10% (volume ratio), and product contains Amount reaches 10wt%, and the product drained is more, and this utility model is reclaimed by concentrator, mother solution temperature can be reduced to 20 DEG C, Isolate the product of 65wt% in mother solution, and drain the mother solution of 10% (volume ratio), the weight of yellow sodium prussiate in the mother solution of discharge Content is 2%, compares original processing mode, is effectively improved product recovery rate.

In sum, the material that this utility model is mainly suitable for needs to meet following condition: 1. indissoluble, slightly soluble or be soluble in Water, product solubility is raised and lowered with the rising of temperature, controls temperature and product can be made to separate out from feed liquid；2. product is through solid Liquid separation equipment isolated.This utility model be suitable for product include aniline-acetonitrile, yellow sodium prussiate, iminodiacetic acid, Iminodiacetonitrile 1,1'-Imidodiacetonitrile, ammonium sulfate, sodium sulfate etc., depending on crystallization kettle, the heating, cooling of concentrator process according to product attribute, its Purpose is to promote that product separates out from feed liquid, such as, when product needed heats up to reduce its dissolubility, and then makes it from feed liquid During precipitation, then the feed liquid in crystallization kettle, concentrator is carried out hyperthermic treatment, otherwise, then carry out cooling process.

Thermal sensitivity product, the product quality that this utility model reclaims and outward appearance are kept consistent with certified products, impurity content Low, it is effectively improved yield and the purity of product, and then increases economic efficiency, it is achieved recovery maximum to product, hence it is evident that Reduce energy consumption, reduce environmental pollution simultaneously.For non-heat-sensitive product, this utility model is also effectively increased the recovery of product Rate, reduces energy consumption, reduces environmental pollution.

Above-described embodiment only illustrative principle of the present utility model and effect thereof are new not for limiting this practicality Type.Above-described embodiment all can be carried out by any person skilled in the art under spirit and the scope of the present utility model Modify or change.Therefore, art has usually intellectual such as without departing from the essence disclosed in this utility model All equivalences completed under god and technological thought are modified or change, and must be contained by claim of the present utility model.

Claims (9)

1. the system of recovered material from crystallization feed liquid, it is characterised in that include crystallization kettle (1), the solid-liquid being sequentially connected with Separation equipment (2), concentrator (3), upper outlet and the lower part outlet of described concentrator (3) are connected to entering of crystallization kettle (1) Mouthful.

The system of recovered material from crystallization feed liquid the most according to claim 1, it is characterised in that described concentrator (3) Upper outlet and crystallization kettle (1) import between be provided with waste liquid outlet.

The system of recovered material from crystallization feed liquid the most according to claim 1, it is characterised in that described concentrator (3) Upper outlet connect have clear liquid transfer tank (4).

The system of recovered material from crystallization feed liquid the most according to claim 1, it is characterised in that described concentrator (3) Lower part outlet and crystallization kettle (1) import between be provided with dope transfering material pump (5).

The system of recovered material from crystallization feed liquid the most according to claim 1, it is characterised in that described concentrator (3) Upper outlet and crystallization kettle (1) import between be provided with clear liquid transfering material pump (6).

The system of recovered material from crystallization feed liquid the most according to claim 1, it is characterised in that described concentrator (3) Number of units be one, two or multiple stage.

The system of recovered material from crystallization feed liquid the most according to claim 1, it is characterised in that described concentrator (3) Number of units be two or during multiple stage, the top of each concentrator (3) is connected in series, the lower part outlet of each concentrator (3) connects Import to crystallization kettle (1).

The system of recovered material from crystallization feed liquid the most according to claim 1, it is characterised in that described crystallization kettle (1) It is provided with production water inlet channel.

The system of recovered material from crystallization feed liquid the most according to claim 1, it is characterised in that described solid-liquid separation sets Standby (2) are centrifuge, filter press, multi-functional pressure filter, suction filtration tank or ceramic filter.