CN208279454U - Navajoite produces Waster water reuse apparatus - Google Patents
Navajoite produces Waster water reuse apparatus Download PDFInfo
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- CN208279454U CN208279454U CN201820626204.XU CN201820626204U CN208279454U CN 208279454 U CN208279454 U CN 208279454U CN 201820626204 U CN201820626204 U CN 201820626204U CN 208279454 U CN208279454 U CN 208279454U
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Abstract
The utility model belongs to technical field of waste water processing, and in particular to a kind of navajoite production Waster water reuse apparatus.Described device, waste water intake pipeline and condensate preheater, vapor preheater and evaporator are sequentially connected, the liquid-phase outlet of evaporator is connected with the import of thickener A, the solvent or diluent outlet of thickener A is connected with the feed inlet of evaporator, the thick material outlet of thickener A is connected with the import of heat centrifugation transfer tank, heat centrifugation transfer tank is sequentially connected with scraper centrifugal machine A and high temperature mother liquor transfer tank, high temperature mother liquor transfer tank outlet respectively with the feed inlet of evaporator, the heat source import of heat exchanger is connected, the thermal source outlet and crystallizing tank of heat exchanger, cold centrifugation transfer tank and thickener B are sequentially connected, the solvent or diluent outlet of thickener B is connected with scraper centrifugal machine B, the thick material outlet of thickener B is connected with two-level piston material pushing centrifugal machine.The utility model structure is simple, scientific and reasonable, and low energy consumption, high-efficient for processing, and it is high to produce purity salt.
Description
Technical field
The utility model belongs to technical field of waste water processing, and in particular to a kind of navajoite production Waster water reuse apparatus.
Background technique
Vanadium has numerous excellent physical properties and chemical property, thus the purposes of vanadium is very extensive, there is metal " dimension life
The title of element ".Initial vanadium is applied to steel mostly, by refining the tissue and crystal grain of steel, grain coarsening temperature is improved, to increase
Add the intensity, toughness and wearability of steel.Later, people gradually had found excellent improving effect of the vanadium in titanium alloy again, and answered
Aerospace field is used, so that aerospace industry made breakthrough progress.With flying for scientific and technological level
Jump development, requirement of the mankind to new material increasingly improve.In non-steel field using more and more extensive, range covers vanadium
The various fields such as aerospace, chemistry, battery, pigment, glass, optics, medicine.
With the increasingly raising of environmental requirement, the production waste of vanadium is badly in need of efficient treatment process.The sewage that navajoite generates
Main component is sodium chloride and ammonium chloride.Sodium chloride is the introducing in calcining of mine ball, enters liquid phase in subsequent extraction vanadic salts.Chlorine
Changing ammonium is the introducing in precipitation, because ammonium metavanadate is precipitating.Final filtration goes out the filtrate of ammonium metavanadate, and as navajoite is main
Production waste.Sodium chloride content is between 5% to 25% in this sewage, and ammonium chloride content is between 7% to 15%.Tradition
Treatment process is only capable of for salinity being steamed out and can not crystallize out salinity sub-prime.In view of navajoite is often in mountain area innerland,
Surrounding solid waste and dangerous waste processing are mating few, and overland transport is extremely inconvenient.
How the production waste of navajoite is effectively handled, and reduce its processing cost as far as possible, becomes this
Field technical problem urgently to be resolved.
In addition, conventional divide salt project using cocrystallization point as discharge criterion, there are two main problems.First, it determines
Control point is a single point after internal circulating load, internal circulating load can not be stable at control point in actual operation.Second, practical supplied materials is past
Toward fluctuation, even if water water quality can monitor in real time, PLC control is also unable to complete Instantaneous Control.It is exactly in the embodiment of real engineering
The unstable of salt quality is produced, is unable to direct reuse into production technology.
Utility model content
According to the above-mentioned deficiencies in the prior art, technical problem to be solved by the utility model is: providing a kind of navajoite life
Waster water reuse apparatus is produced, structure is simple, scientific and reasonable, and low energy consumption, high-efficient for processing, produces purity salt height, being capable of direct reuse
Calcining and precipitation process section to navajoite, turn waste into wealth.
The technical scheme adopted by the utility model to solve the technical problem is as follows:
The navajoite produces Waster water reuse apparatus, including waste water intake pipeline, and waste water intake pipeline and condensate preheat
Device, vapor preheater and evaporator are sequentially connected, and the liquid-phase outlet of evaporator is connected with the import of thickener A, and thickener A's is dilute
Material outlet is connected with the feed inlet of evaporator, and the thick material outlet of thickener A is connected with the import of heat centrifugation transfer tank, in heat centrifugation
Turn tank to be sequentially connected with scraper centrifugal machine A and high temperature mother liquor transfer tank, high temperature mother liquor transfer tank outlet respectively with evaporator
Feed inlet, heat exchanger heat source import be connected, the thermal source outlet of heat exchanger and crystallizing tank, cold centrifugation transfer tank and thickener B according to
Secondary to be connected, the solvent or diluent outlet of thickener B is connected with scraper centrifugal machine B, and the outlet of thick material and the Double -stagepusher of thickener B is centrifuged
Machine is connected, and scraper centrifugal machine B and two-level piston material pushing centrifugal machine are connected with low temperature mother liquor transfer tank respectively, low temperature mother liquor transfer tank
Outlet be connected with the cold source import of heat exchanger, the outlet of the cold source of heat exchanger is connected with waste water intake pipeline.
Wherein:
The condensate preheater is composed in series by condensate preheater A and condensate preheater B.Condensate preheater A and condensate
Preheater B preheats material using condensate.
The vapor preheater preheats material using raw steam, and in vapor preheater, material is preheated to
Evaporate bubble point.
The evaporator is sequentially connected in series by evaporator A, evaporator B and evaporator C.
Set collet outside the described heat centrifugation transfer tank, raw steam insulation be passed through in collet, prevent ammonium chloride heat from
Turn in the heart to be precipitated in tank.
The scraper centrifugal machine A is composed in parallel by scraper centrifugal machine A-1 and scraper centrifugal machine A-2.
The crystallizing tank is by crystallizing tank A, crystallizing tank B, crystallizing tank C, crystallizing tank D, crystallizing tank E and crystallizing tank F parallel connection group
At.
Using the technique of above-mentioned apparatus, its step are as follows:
1) sodium chloride produces salt section: waste water is sequentially sent to condensate preheater and vapor preheater after mixing with ammonium chloride mother liquor
Preheating, material after preheating are sent into evaporative crystallization in evaporator, and the magma after concentration is pumped into thickener A, thickness material be sent into heat from
Turn tank in the heart, solvent or diluent sends evaporator back to, and thickness material is centrifuged through scraper centrifugal machine A produces sodium chloride, and chlorination mother liquid of sodium enters high temperature mother liquor
It is stored in transfer tank, a part, which returns to, to continue to evaporate in evaporator, and another part enters ammonium chloride and produces salt section；
2) ammonium chloride produces salt section: chlorination mother liquid of sodium exchanges heat in heat exchanger first with ammonium chloride mother liquor, after cooling
Chlorination mother liquid of sodium enters in crystallizing tank, and the material after crystallization is sent to cold centrifugation transfer tank, and after thickener B separation, thickness material is sent into
Two-level piston material pushing centrifugal machine carries out centrifugation and produces ammonium chloride, and solvent or diluent is sent into scraper centrifugal machine B centrifugation and produces ammonium chloride, ammonium chloride mother liquor
Into being stored in low temperature mother liquor transfer tank, it is then pumped into heat exchanger and exchanges heat with chlorination mother liquid of sodium, the ammonium chloride after heat exchange
Mother liquor enters sodium chloride and produces salt section.
The step of described evaporative crystallization, in the project that steam is had more than needed, it is possible to use multiple-effect evaporation technique.
Magma temperature after the concentration is 80-120 DEG C.
It is accounted by technique it is found that magma solid volume content after being concentrated is 8-15%, is centrifuged using Double -stagepusher
Machine is easy to produce phenomenon of having loose bowels.Salt quality is produced to improve sodium chloride, and guarantees the yield of mother liquor.The centrifuge of sodium chloride production salt section
It is used alternatingly using two scraper centrifugal machines.
The temperature of the crystallizing tank is 20-40 DEG C.
Since the ammonium chloride of output needs to be multiplexed into precipitation process section, purity needs to be higher than 95%, to reduce mother liquor
Middle impurity to ammonium chloride produce salt influence, ammonium chloride produce salt section centrifuging process section select two kinds of centrifuges to ammonium chloride magma into
Row centrifugation.The thick material that stiff goes out is sent to being centrifuged in two-level piston material pushing centrifugal machine, and solvent or diluent is sent to being centrifuged in scraper centrifugal machine B.
The chlorination mother liquid of sodium of salt section is produced into ammonium chloride and enters the internal circulating load use that sodium chloride produces salt section ammonium chloride mother liquor
Following method calculates:
A, the ammonium chloride component and sodium chloride component in chlorination mother liquid of sodium and ammonium chloride mother liquor are calculated respectively；
B, using the available section of ammonium chloride component and sodium chloride component, to whole under specified feed component rated capacity
A process carries out MaterialBalance Computation, obtains the bound of Recycling Mother Solution amount；
C, after the Recycling Mother Solution amount section of multiple feed components takes intersection, operable section is obtained.
Compared with prior art, the utility model has the beneficial effects that
1, apparatus structure described in the utility model is simple, scientific and reasonable, and low energy consumption, high-efficient for processing, produces purity salt height,
Up to 95% or more, can calcining and precipitation process section of the direct reuse to navajoite, turn waste into wealth
2, energy consumption saving.Compared with tradition evaporation, increased energy consumption is less than 5%.
3, technique applicability is good.The water of different saliferous ratios is handled without using covering equipment more.
Detailed description of the invention
Fig. 1 is utility model device structural schematic diagram；
In figure: 1, condensate preheater；2, vapor preheater；3, evaporator；4, thickener A；5, heat centrifugation transfer tank；6, it presss from both sides
Set；7, scraper centrifugal machine A；8, high temperature mother liquor transfer tank；9, heat exchanger；10, crystallizing tank；11, cold centrifugation transfer tank；12, stiff
Device B；13, two-level piston material pushing centrifugal machine；14, scraper centrifugal machine B；15, low temperature mother liquor transfer tank.
Specific embodiment
The embodiments of the present invention are described further with reference to the accompanying drawing:
Embodiment
As shown in Figure 1, the navajoite produces Waster water reuse apparatus, including waste water intake pipeline, waste water intake pipeline
It is sequentially connected with condensate preheater 1, vapor preheater 2 and evaporator 3, the import of the liquid-phase outlet and thickener A4 of evaporator 3
It is connected, the solvent or diluent outlet of thickener A4 is connected with the feed inlet of evaporator 3, the outlet of thick material and the heat centrifugation transfer tank of thickener A4
5 import is connected, and heat centrifugation transfer tank 5 and scraper centrifugal machine A7 and high temperature mother liquor transfer tank 8 are sequentially connected, high temperature mother liquor transfer
The outlet of tank 8 is connected with the heat source import of the feed inlet of evaporator 3, heat exchanger 9 respectively, the thermal source outlet of heat exchanger 9 and crystallization
Tank 10, cold centrifugation transfer tank 11 and thickener B12 are sequentially connected, solvent or diluent outlet and the scraper centrifugal machine B14 phase of thickener B12
Even, the thick material outlet of thickener B12 is connected with two-level piston material pushing centrifugal machine 13, scraper centrifugal machine B14 and Double -stagepusher
Centrifuge 13 is connected with low temperature mother liquor transfer tank 15 respectively, the outlet of low temperature mother liquor transfer tank 15 and the cold source import of heat exchanger 9
It is connected, the cold source outlet of heat exchanger 9 is connected with waste water intake pipeline.
Wherein:
The condensate preheater 1 is composed in series by condensate preheater A and condensate preheater B.Condensate preheater A and condensate
Preheater B preheats material using condensate.
The vapor preheater 2 preheats material using raw steam, and in vapor preheater 2, material is preheated
To evaporation bubble point.
The evaporator 3 is sequentially connected in series by evaporator A, evaporator B and evaporator C.
Collet 6 is set outside the heat centrifugation transfer tank 5, raw steam insulation is passed through in collet 6, prevents ammonium chloride in heat
It is precipitated in centrifugation transfer tank 5.
The scraper centrifugal machine A7 is composed in parallel by scraper centrifugal machine A-1 and scraper centrifugal machine A-2.
The crystallizing tank 10 is in parallel by crystallizing tank A, crystallizing tank B, crystallizing tank C, crystallizing tank D, crystallizing tank E and crystallizing tank F
Composition.
Using the technique of above-mentioned apparatus, steps are as follows:
1) sodium chloride produces salt section: waste water is sequentially sent to condensate preheater and vapor preheater after mixing with ammonium chloride mother liquor
Preheating, material after preheating are sent into evaporative crystallization in evaporator, and the magma after concentration is pumped into thickener A, thickness material be sent into heat from
Turn tank in the heart, solvent or diluent sends evaporator back to, and thickness material is centrifuged through scraper centrifugal machine A produces sodium chloride, and chlorination mother liquid of sodium enters high temperature mother liquor
It is stored in transfer tank, a part, which returns to, to continue to evaporate in evaporator, and another part enters ammonium chloride and produces salt section；
2) ammonium chloride produces salt section: chlorination mother liquid of sodium exchanges heat in heat exchanger first with ammonium chloride mother liquor, after cooling
Chlorination mother liquid of sodium enters in crystallizing tank, and the material after crystallization is sent to cold centrifugation transfer tank, and after thickener B separation, thickness material is sent into
Two-level piston material pushing centrifugal machine carries out centrifugation and produces ammonium chloride, and solvent or diluent is sent into scraper centrifugal machine B centrifugation and produces ammonium chloride, ammonium chloride mother liquor
Into being stored in low temperature mother liquor transfer tank, it is then pumped into heat exchanger and exchanges heat with chlorination mother liquid of sodium, the ammonium chloride after heat exchange
Mother liquor enters sodium chloride and produces salt section.
Magma temperature after the concentration is 100 DEG C.
The temperature of the crystallizing tank is 35 DEG C.
It is adopted into the internal circulating load that ammonium chloride produces the chlorination mother liquid of sodium of salt section and enters the ammonium chloride mother liquor that sodium chloride produces salt section
It calculates with the following method:
A, the ammonium chloride component and sodium chloride component in chlorination mother liquid of sodium and ammonium chloride mother liquor are calculated respectively；
B, using the available section of ammonium chloride component and sodium chloride component, to whole under specified feed component rated capacity
A process carries out MaterialBalance Computation, obtains the bound of Recycling Mother Solution amount；
C, after the Recycling Mother Solution amount section of multiple feed components takes intersection, operable section is obtained.
For 100 DEG C of chlorination mother liquid of sodium, 35 DEG C of ammonium chloride mother liquor, citing design is carried out to the unit of 4 tons/h evaporation capacity.
High temperature mother liquor as described below is chlorination mother liquid of sodium, and the low temperature mother liquor is ammonium chloride mother liquor.
1, consult physical property handbook obtain at 100 DEG C and at 35 DEG C ammonium chloride and chlorination mother liquid of sodium total dissolubility data.
Table 1
| NH4Cl | NACl | H2O | |
| 100℃R1G | 34.13 | 10.82 | 55.05 |
| 100℃R2 | 30.1 | 13.04 | 56.86 |
In table 1,100 DEG C of R1G rows are pointed out that the quality dissolution of ammonium chloride and sodium chloride near cocrystallization point at 100 DEG C
Percentage is spent, 100 DEG C of R1G are denoted as.100 DEG C of R2 rows are pointed out that ammonium chloride and sodium chloride are in the list for being biased to sodium chloride at 100 DEG C
One reference point of phase crystal region, the quality solubility percentage of ammonium chloride and sodium chloride near the reference point.
Table 2
| NH4Cl | NACl | H2O | |
| 35℃R1G | 18.25 | 15.75 | 66 |
| 35℃R2 | 20.38 | 13.24 | 66.38 |
Similarly, be pointed out that in table 2 ammonium chloride and sodium chloride at 35 DEG C near cocrystallization point and be biased to ammonium chloride list
Two reference points of phase crystal region are denoted as 35 DEG C of R1G and 35 DEG C of R2 respectively.
2, after obtaining 4 reference points, we need to only go out the mother liquor group that sodium chloride and low temperature only go out ammonium chloride to high temperature is met
Divide and is calculated.Meet this needs, makes ammonium chloride in not higher than 100 DEG C R1G of the mass percent of ammonium chloride in 100 DEG C of mother liquors
Mass percent, while in view of actual items water quality is complicated, this method and without using more advanced model to reference point with
Outer point carries out calculation.For the error for reducing equal difference method, this method is only by the ammonium chloride and sodium chloride content of 100 DEG C of mother liquors
Control is in 100 DEG C of R1G and 100 DEG C of R2 between ammonium chloride and sodium chloride content.Similarly, sodium chloride and ammonium chloride in 35 DEG C of mother liquors
Content control is in 35 DEG C of R1G and 35 DEG C of R2 between ammonium chloride and sodium chloride content.
3, table 3 and table 4 can be obtained by the EQUILIBRIUM CALCULATION FOR PROCESS of Microsoft Excel again.
Table 3
In table 3, the mass percent of ammonium chloride has reached 34% in 100 DEG C of mother liquors, very approaching cocrystallization point, simultaneously
There are also 2% or more for sodium chloride content in 35 DEG C of mother liquors in 35 DEG C of R1G of sodium chloride content distance.What table 3 was stated is to meet 100
The mother liquor composition of DEG C single phase crystalline as under the premise of.
Table 4
In table 4, the mass percent of sodium chloride has reached 15.21% in 35 DEG C of mother liquors, very approaching cocrystallization point, together
When 100 DEG C of mother liquors in chlorination ammonia content in 100 DEG C of R1G of ammonium chloride content distance there are also 4% or more.What table 4 was stated is with full
Mother liquor composition of the 35 DEG C of single phase crystallines of foot as under the premise of.
4, with the component of mother liquor in different feed component combination tables 3 and table 4, the lower limit of Recycling Mother Solution amount and upper is obtained
Limit.Table 5 and table 6 can be obtained for feeding containing 11.5% ammonium chloride and 20% sodium chloride.
Table 5
Table 6
Indicate that respective material is put down under table 3 and the given high temperature of table 4 and low temperature mother liquor component respectively by table 5 and table 6
Weigh situation.In conjunction with the Recycling Mother Solution gross mass of table 5 and table 6 it is found that being 11.5% ammonium chloride and 20% chlorine in feed component
Change sodium, in the case that evaporation capacity is 4000kg/h, evaporates mother liquor, i.e. high temperature mother liquor, discharge rate is in 3952kg/h-4833kg/h model
It encloses the interior high temperature that is able to achieve and goes out sodium chloride, low temperature goes out the process goal of ammonium chloride.
5, table 7 can be obtained after being calculated various ingredients according to the above method.
Table 7
By the way that the section of multiple groups high temperature Recycling Mother Solution amount is taken intersection, the tolerable wave zone of influent quality can be sought
Between, facilitate the technology controlling and process for instructing preceding working procedure.As shown in Table 7, the Feedstock fluctuation of ammonium chloride influences pole to the internal circulating load of mother liquor
Greatly, opposite influence of the sodium chloride to Feedstock fluctuation to Recycling Mother Solution amount is smaller.To the guidance of practical operation be preceding road as far as possible
Stablize the input concentration of ammonium chloride.
To sum up, what the technique and design method were mainly evaded is in conventional sub-prime crystallization design process with single material balance
Point is used as design considerations.Single equilibrium data table can realize that sub-prime crystallizes in technique is accounted, but implement to its in Practical Project
It is totally unfavorable to user.The reason is that single material balance can not be met in water quality and equipment actual motion that user provides
The material balance that table is stated.And single material balance table often deviates water quality, and the operating point after evaporation capacity deviates changes,
There is no directive function.User often finds it hard to tell about one's suffering, and while bearing a loss, situation is not yet in the disputes act with Party B
Benefit.This technique is solving the problems, such as navajoite utilization of wastewater resource at the same time, it is desirable to the design that can be crystallized to the sub-prime of other industry
Thinking is casted a brick to attract jade.
Claims (6)
1. a kind of navajoite produces Waster water reuse apparatus, including waste water intake pipeline, it is characterised in that: waste water intake pipeline and solidifying
Water preheater (1), vapor preheater (2) and evaporator (3) are sequentially connected, the liquid-phase outlet of evaporator (3) and thickener A (4)
Import be connected, the outlet of the solvent or diluent of thickener A (4) is connected with the feed inlet of evaporator (3), the thick material of thickener A (4) export and
The import of heat centrifugation transfer tank (5) is connected, heat centrifugation transfer tank (5) and scraper centrifugal machine A (7) and high temperature mother liquor transfer tank (8)
It is sequentially connected, the outlet of high temperature mother liquor transfer tank (8) the heat source import phase with the feed inlet of evaporator (3), heat exchanger (9) respectively
Even, thermal source outlet and crystallizing tank (10), cold centrifugation transfer tank (11) and the thickener B (12) of heat exchanger (9) are sequentially connected, stiff
The solvent or diluent outlet of device B (12) is connected with scraper centrifugal machine B (14), the thick material of thickener B (12) export and Double -stagepusher from
Scheming (13) is connected, scraper centrifugal machine B (14) and two-level piston material pushing centrifugal machine (13) respectively with low temperature mother liquor transfer tank (15)
Be connected, the outlet of low temperature mother liquor transfer tank (15) is connected with the cold source import of heat exchanger (9), the cold source of heat exchanger (9) export and
Waste water intake pipeline is connected.
2. navajoite according to claim 1 produces Waster water reuse apparatus, it is characterised in that: the condensate preheater
(1) it is composed in series by condensate preheater A and condensate preheater B.
3. navajoite according to claim 1 produces Waster water reuse apparatus, it is characterised in that: the evaporator (3) by
Evaporator A, evaporator B and evaporator C are sequentially connected in series.
4. navajoite according to claim 1 produces Waster water reuse apparatus, it is characterised in that: the heat centrifugation transfer tank
(5) external to set collet (6).
5. navajoite according to claim 1 produces Waster water reuse apparatus, it is characterised in that: the scraper centrifugal machine A
(7) it is composed in parallel by scraper centrifugal machine A-1 and scraper centrifugal machine A-2.
6. navajoite according to claim 1 produces Waster water reuse apparatus, it is characterised in that: the crystallizing tank (10) by
Crystallizing tank A, crystallizing tank B, crystallizing tank C, crystallizing tank D, crystallizing tank E and crystallizing tank F are composed in parallel.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820626204.XU CN208279454U (en) | 2018-04-27 | 2018-04-27 | Navajoite produces Waster water reuse apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820626204.XU CN208279454U (en) | 2018-04-27 | 2018-04-27 | Navajoite produces Waster water reuse apparatus |
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| CN208279454U true CN208279454U (en) | 2018-12-25 |
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ID=64752541
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108298758A (en) * | 2018-04-27 | 2018-07-20 | 徐翔 | Navajoite produces Waster water reuse apparatus and its technique |
-
2018
- 2018-04-27 CN CN201820626204.XU patent/CN208279454U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108298758A (en) * | 2018-04-27 | 2018-07-20 | 徐翔 | Navajoite produces Waster water reuse apparatus and its technique |
| CN108298758B (en) * | 2018-04-27 | 2024-04-12 | 江苏和诚制药设备制造有限公司 | Vanadium ore production wastewater recycling device and process thereof |
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