CN107913526A - High level salt solution evaporation crystallization equipment and process - Google Patents
High level salt solution evaporation crystallization equipment and process Download PDFInfo
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- CN107913526A CN107913526A CN201711454774.1A CN201711454774A CN107913526A CN 107913526 A CN107913526 A CN 107913526A CN 201711454774 A CN201711454774 A CN 201711454774A CN 107913526 A CN107913526 A CN 107913526A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0018—Evaporation of components of the mixture to be separated
- B01D9/0031—Evaporation of components of the mixture to be separated by heating
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
Abstract
The present invention provides a kind of high level salt solution evaporation crystallization equipment and process, it is related to the technical field of evaporative crystallization, including：Falling film heating room is equipped with falling film heating room liquid outlet opening, the vapour liquid separator liquid inlet opening connection of falling film heating room liquid outlet opening and vapour liquid separator；Vapour liquid separator is equipped with the first liquid outlet opening of vapour liquid separator, and a part of liquid come out from vapour liquid separator enters crystal separator by the first liquid outlet opening of vapour liquid separator；Crystal separator circulation discharge port is provided with crystal separator, crystal separator circulation discharge port is connected with forced circulation heating chamber；Entered by the feed liquid after forced circulation oven heats in liquid-solid separator and carry out separation of solid and liquid；Forced circulation heating chamber is recycled into by solid phase in the liquid of solid-liquor separation solid-liquid separation, enters crystal separator by liquid phase in the liquid of solid-liquor separation solid-liquid separation, the technical problem for solving high energy consumption fouling.
Description
Technical field
The present invention relates to evaporative crystallization technique field, more particularly, to a kind of high level salt solution evaporation crystallization equipment and technique side
Method.
Background technology
Evaporative distillation is widely used in dirt, wastewater treatment, chemical industry, pharmacy, food, sea water desalination, salt manufacturing etc. and is related to evaporation
All conglomeraties of technique.Evaporative distillation is the process of a high energy consumption, and evaporation technology is the big power consumer in these industries.These rows
The main productive consumption of industry is energy consumption cost.
Big technique is fluctuated except the requirement of some special process, boiling point rise especially high, material, newly-built evaporation process is big at present
Use MVR evaporation technologies more.
And MVR now there are the problem of be concentrated mainly on：Compressor heating limited ability system, domestic stable operation at present
Substantially below 20 DEG C, import fan temperature rise, using two-stage to thtee-stage shiplock, can tackle the temperature rise of big flow compressor at 8 DEG C
Boiling point rise it is limited；Evaporation process is big by heating chamber scale effect, scale effect heat transfer, and then influences evaporation MVR vapo(u)rization systems
Dynamic equilibrium, cause whole MVR system operations to be collapsed；Reliability, is related to the stabilization of the mechanical performance of compressor, evaporation
The stabilization of device heat transfer property, compressor and the matched stabilization of evaporator.
Function of mechanical steam recompression (Mechanical Vapor Recompression, MVR) heat pump techniques, are the current country
The outer most advanced most energy saving technology in evaporation field.Its principle is the indirect steam produced using vapour compression machine Compression Evaporation,
Electric energy is converted into thermal energy, improves the enthalpy of indirect steam, and the indirect steam for being enhanced thermal energy returns to vaporization chamber and heated, to reach
The potential of indirect steam is recycled, so as to which exterior raw steam is not required, realizes that evaporation is dense by evaporator self-loopa
The purpose of contracting.It can be said that MVR evaporators are a processes marketed one's own products.In practical operation, pass through PLC, microcontroller, group
The forms such as state come control system temperature, pressure motor rotating speed, keep system evaporation balance.
The information for being disclosed in the background section is merely intended to deepen the understanding of the general background technology to the present invention, and
It is not construed as recognizing or implies the information structure prior art known to those skilled in the art in any form.
The content of the invention
It is an object of the invention to provide high level salt solution evaporation crystallization equipment and process, to alleviate in the prior art
Existing high energy consumption, the technical problem of easy fouling.
In a first aspect, a kind of high level salt solution evaporation crystallization equipment provided by the invention, including：Falling film heating room, vapour-liquid point
From device, crystal separator, forced circulation heating chamber and liquid-solid separator；
The falling film heating room for heating raw material is equipped with falling film heating room liquid outlet opening, falling film heating room liquid
Body discharge port is connected with the vapour liquid separator liquid inlet opening of the vapour liquid separator；
The vapour liquid separator for vapor-liquid separation is equipped with the first liquid outlet opening of vapour liquid separator, from the vapour-liquid point
A part of liquid come out from device enters the crystal separator by first liquid outlet opening of vapour liquid separator；
Be provided with crystal separator circulation discharge port on the crystal separator, crystal separator circulation discharge port with
The forced circulation heating chamber connection；
Entered by the feed liquid after the forced circulation oven heats in the liquid-solid separator and carry out separation of solid and liquid；
The forced circulation heating chamber is recycled into by solid phase in the liquid of the solid-liquor separation solid-liquid separation；
Enter the crystal separator by liquid phase in the liquid of the solid-liquor separation solid-liquid separation；In the crystallization point
From vapor-liquid separation is carried out in device, discharged after crystal grain crystallization.
Further, inert particle is added with before the forced circulation heating chamber is entered, the inert particle is existed
Circulated between the forced circulation heating chamber and the liquid-solid separator.
Further, the inert particle is the material not reacted with raw material.
Further, enter in first liquid outlet opening of vapour liquid separator on the circulation passage of the crystal separator
It is provided with punishment in advance pump.
Further, the crystal separator circulation discharge port is pumped with the forced circulation heating chamber by secondary cycle connects
Connect.
Further, another part liquid come out from the vapour liquid separator passes through the vapour liquid separator second liquid
Discharge port is back to the falling film heating room.
Further, after the vapour liquid separator and the crystal separator carry out vapor-liquid separation, in the vapor-liquid separation
Device top is provided with vapour liquid separator steam (vapor) outlet, and the crystal separator top is provided with crystal separator steam (vapor) outlet；
Enter level-one pressure after the steam mixing that the vapour liquid separator steam (vapor) outlet and crystal separator steam (vapor) outlet come out
Contracting machine is compressed, and compressed a part of steam enters the falling film heating room.
Further, the lower part of the falling film heating room is provided with falling film heating room condensation-water drain, from the falling liquid film
The condensed water of heating chamber condensation-water drain outflow condenses water preheater by level-one and raw material is heated.
Second aspect, a kind of process provided by the invention, including：High level salt solution evaporative crystallization described in first aspect
Equipment；
Raw material enters from head tank by feed pump, after level-one condenses water preheater and the heating of B-grade condensation water preheater
Enter vapour liquid separator after being heated into falling film heating room and carry out vapor-liquid separation；One after vapour liquid separator vapor-liquid separation
Liquid separation body is back to falling film heating room through primary cycle pump, and another part liquid enters crystal separator through punishment in advance pump, from crystallization
Feed liquid in separator out enters forced circulation heating chamber after being mixed by secondary cycle pump with inert particle, passes through heating chamber
Feed liquid after heating enters liquid-solid separator and carries out solid-liquor separation, and solid phase is recycled in forced circulation heating chamber, is followed into pressure
Inert particle separation in ring heating chamber, liquid phase enter crystal separator and carry out vapor-liquid separation；
After raw material carries out vapor-liquid separation in vapour liquid separator and crystal separator, indirect steam is mixed into one stage of compression
Machine is compressed, and steam after compression is partly into falling film heating room as heat source, and the condensed water of generation is through level-one
Condensation water preheater preheats raw material, and another part is further compressed into split-compressor, again compressed steam
Raw material is preheated through B-grade condensation water preheater as heat source, the condensed water of generation into forced circulation heating chamber.
Using a kind of high level salt solution evaporation crystallization equipment provided by the invention, including：Falling film heating room, vapour liquid separator,
Crystal separator, forced circulation heating chamber and liquid-solid separator；Falling film heating room for heating raw material is equipped with falling film heating room
The vapour liquid separator liquid inlet opening connection of liquid outlet opening, falling film heating room liquid outlet opening and vapour liquid separator；For vapour
The separated vapour liquid separator of liquid is equipped with the first liquid outlet opening of vapour liquid separator, and a part of liquid come out from vapour liquid separator leads to
Cross first liquid outlet opening of vapour liquid separator and enter the crystal separator；Crystal separator is provided with crystal separator
Discharge port is circulated, crystal separator circulation discharge port is connected with forced circulation heating chamber；After forced circulation oven heats
Feed liquid enter liquid-solid separator in carry out separation of solid and liquid；It is recycled into by solid phase in the liquid of solid-liquor separation solid-liquid separation
Forced circulation heating chamber, and discharged after the solid-phase crystallization entered after forced circulation heating chamber；By solid-liquor separation solid-liquid separation
Liquid in liquid phase enter crystal separator.
Here high level salt solution evaporation crystallization equipment, than the evaporation boiling point liter of common MVR vapo(u)rization systems at present on the market
Solution within 15 DEG C, high level salt solution evaporation crystallization equipment reply boiling point provided by the invention rise more than 15 DEG C of solution, because
This improves efficiency, and relative to also having more preferable ant-scaling effect in the prior art.Facility compact, floor space is small,
Required space is small, and the heating chamber that the indirect steam for evaporating generation is sent to evaporator after compression makes material as heating steam use
Liquid maintains fluidized state, and heats steam and be then condensed into water in itself.Originally the steam to be discarded is obtained for sufficient utilization, returns
Latent heat has been received, and has improved the thermal efficiency.The present invention on the basis of existing technology, is rationally designed, further increases steaming
The energy saving economy of hair crystallization technique, globality, reasonability, flexibility.
Process provided by the invention, has the advantages that above-mentioned high level salt solution evaporation crystallization equipment has all.
Brief description of the drawings
, below will be to specific in order to illustrate more clearly of the specific embodiment of the invention or technical solution of the prior art
Embodiment or attached drawing needed to be used in the description of the prior art are briefly described, it should be apparent that, in describing below
Attached drawing is some embodiments of the present invention, for those of ordinary skill in the art, before not making the creative labor
Put, other attached drawings can also be obtained according to these attached drawings.
Fig. 1 is process flow chart provided in an embodiment of the present invention.
Icon：100- falling film heatings room；110- falling film heatings room liquid outlet opening；120- falling film heatings room condensed water
Outlet；200- vapour liquid separators；210- vapour liquid separator liquid inlet openings；The first liquid outlet opening of 220- vapour liquid separators；
230- vapour liquid separator second liquid discharge ports；240- vapour liquid separator steam (vapor) outlets；300- crystal separators；310- is tied
Brilliant separator circulation discharge port；320- crystal separator steam (vapor) outlets；400- forced circulation heating chambers；410- forced circulations
Heating chamber condensate outlet；500- liquid-solid separators；600- punishments in advance pump；700- secondary cycles pump；800- stage compressors；
900- level-ones condense water preheater；1000- split-compressors；1100- B-grade condensation water preheaters；1300- feed pumps；
1400- primary cycles pump.
Embodiment
Technical scheme is clearly and completely described below in conjunction with attached drawing, it is clear that described implementation
Example is part of the embodiment of the present invention, instead of all the embodiments.Based on the embodiments of the present invention, ordinary skill
Personnel's all other embodiments obtained without making creative work, belong to the scope of protection of the invention.
In the description of the present invention, it is necessary to explanation, term " " center ", " on ", " under ", "left", "right", " vertical ",
The orientation or position relationship of the instruction such as " level ", " interior ", " outer " be based on orientation shown in the drawings or position relationship, merely to
Easy to describe the present invention and simplify description, rather than instruction or imply signified device or element must have specific orientation,
With specific azimuth configuration and operation, therefore it is not considered as limiting the invention.In addition, term " first ", " second ",
" the 3rd " is only used for description purpose, and it is not intended that instruction or hint relative importance.
In the description of the present invention, it is necessary to illustrate, unless otherwise clearly defined and limited, term " installation ", " phase
Even ", " connection " should be interpreted broadly, for example, it may be being fixedly connected or being detachably connected, or be integrally connected；Can
To be mechanical connection or be electrically connected；It can be directly connected, can also be indirectly connected by intermediary, Ke Yishi
Connection inside two elements.For the ordinary skill in the art, with concrete condition above-mentioned term can be understood at this
Concrete meaning in invention.
The embodiment of the present invention is described in detail below in conjunction with attached drawing.It should be appreciated that this place is retouched
The embodiment stated is merely to illustrate and explain the present invention, and is not intended to limit the invention.
Fig. 1 is refer to, below in conjunction with attached drawing to high level salt solution evaporation crystallization equipment provided in an embodiment of the present invention and work
Process elaborates.
A kind of high level salt solution evaporation crystallization equipment provided by the invention, including：Falling film heating room 100, vapour liquid separator
200th, crystal separator 300, forced circulation heating chamber 400 and liquid-solid separator 500；
The falling film heating room 100 for heating raw material is equipped with falling film heating room liquid outlet opening 110, falling film heating room
Liquid outlet opening 110 is connected with the vapour liquid separator liquid inlet opening 210 of vapour liquid separator 200；
Vapour liquid separator for vapor-liquid separation is equipped with the first liquid outlet opening of vapour liquid separator 220, from vapour liquid separator
A part of liquid out enters crystal separator 300 by the first liquid outlet opening of vapour liquid separator 220；
Crystal separator circulation discharge port 310, crystal separator circulation discharge port 310 are provided with crystal separator 300
It is connected with forced circulation heating chamber 400；
Feed liquid after being heated by forced circulation heating chamber 400, which enters, carries out separation of solid and liquid in liquid-solid separator 500；
Solid phase is recycled into forced circulation heating chamber 400 in liquid by 500 separation of solid and liquid of liquid-solid separator；
Liquid phase enters crystal separator 300 in liquid by 500 separation of solid and liquid of liquid-solid separator；In crystal separator
Vapor-liquid separation is carried out in 300, is discharged after crystal grain crystallization.
It should be noted that high level salt solution evaporation crystallization equipment here, than common MVR vapo(u)rization systems at present on the market
Evaporation boiling point rise solution below 15 DEG C, high level salt solution evaporation crystallization equipment reply boiling point provided by the invention rise 15 DEG C with
On solution, therefore improve efficiency.Facility compact, floor space is small, required space is small, evaporates the indirect steam of generation through pressure
The heating chamber that evaporator is sent to after contracting is used as heating steam, feed liquid is maintained fluidized state, and it is then cold in itself to heat steam
Congeal into water.Originally the steam to be discarded is obtained for sufficient utilization, has recycled latent heat, and improve the thermal efficiency.The present invention is extremely
Few one embodiment on the basis of existing technology, is rationally designed, further increases the energy saving warp of evaporative crystallization technique
Ji property, globality, reasonability, flexibility.
Forced circulation heating chamber 400 is connected with vacuum pump so that forced circulation heating chamber 400 is become vacuum equipment.
Specifically, the solid phase in forced circulation heating chamber is divided into two kinds：Inert particle and crystalline particle, crystal grain than
Small more of inert particle, from forced circulation heating chamber come out after liquid enter liquid-solid separator, by liquid-solid separator separation energy
The limitation of power, this separating capacity determine that crystal grain will not be separated originally substantially when designing liquid-solid separator, separation
Essentially inert particle, crystal grain out enters crystal separator with liquid phase, vapor-liquid separation is carried out in crystal separator,
Continued cycling through from liquid-solid separator by separated inert particle into circulation pipe.
It should be noted that the lower perforated plate in forced circulation heating chamber is provided with particle distributor, particle point is provided with
Forced circulation heating chamber after cloth device can make inert particle distribution more uniform.Here particle distributor is using orifice-plate type point
Cloth device, the distribution in hole is small in median pore radius, and aperture becomes larger what is be distributed around.
In addition, being added with inert particle before forced circulation heating chamber 400 is entered, inert particle is set to add in forced circulation
Circulated between hot cell 400 and liquid-solid separator 500.
It should be noted that after addition inert particle, inert particle circulation, inertia grain in forced circulation heating chamber 400
The shear stress that subflow produces during moving delays the formation of dirty layer, while the flow process augmentation of heat transfer of inert particle, and increase passes
The thermal efficiency.
Here add the inert particle used and be different from conventional selection, selection is mixed inert particle, polytetrafluoroethylene (PTFE)
With the mixture of silica, and the ratio of silica and polytetrafluoroethylene (PTFE) is：4% -30%；As ratio can be：4%th,
8%th, 12%, 16%, 20%, 24%, 28% or 30%, but be not limited to that.Such mixed inert particle both had
The hardness of silica, but density is small, so as to need the little energy consumed when circulating.Compare relative to polytetrafluoroethylene (PTFE), gather
Although tetrafluoroethene corrosivity is good, hardness wears no resistance.So not only hardness is good at the same time for the inert particle of the invention selected
Also there is stronger corrosion resistance, therefore can adapt to more operating modes.
Here the selection of inert particle in flow process mainly by producing flow-disturbing, so that the shear stress produced prolongs
The formation of slow dirt layer, has reached the effect of good antiscale property.
In addition, the particle diameter of inert particle is 1mm-5mm.
It should be noted that the particle size of inert particle is：1mm, 2mm, 3mm, 4mm or 5mm, provide in the present invention
High level salt solution evaporation crystallization equipment selection particle size range in, and the material selection of the inert particle selected here for original
Expect the material not reacted.
It is provided with addition, entering in the first liquid outlet opening of vapour liquid separator 220 on the circulation passage of crystal separator 300
Punishment in advance pump 600.
Specifically, crystal separator circulation discharge port 310 is connected with forced circulation heating chamber 400 by secondary cycle pump 700
Connect.Another part liquid that institute's vapour liquid separator comes out is back to falling liquid film by vapour liquid separator second liquid discharge port 230 and adds
Hot cell 100.After vapour liquid separator 200 and crystal separator 300 carry out vapor-liquid separation, it is provided with 200 top of vapour liquid separator
Vapour liquid separator steam (vapor) outlet 240, crystal separator steam (vapor) outlet 320 is provided with 300 top of crystal separator；
Enter level-one after the steam mixing that vapour liquid separator steam (vapor) outlet 240 and crystal separator steam (vapor) outlet 320 come out
Compressor 800 is compressed, and compressed a part of steam enters falling film heating room 100.
The lower part of falling film heating room 100 is provided with falling film heating room condensation-water drain 120, and from falling film heating room, condensed water goes out
The condensed waters of the outflow of mouth 120 condense water preheater 900 by level-one and raw material are heated.
Enter level-one after the steam mixing that vapour liquid separator steam (vapor) outlet 240 and crystal separator steam (vapor) outlet 320 come out
Compressor 800 is compressed, and compressed another part steam is entered by 1000 compressed steam of split-compressor to be forced
Circulating-heating room 400.
The lower part of forced circulation heating chamber 400 is provided with forced circulation heating chamber condensate outlet 410, forced circulation heating
The condensed water that room condensate outlet 410 produces carries out secondary preheating by B-grade condensation water preheater 1100 to raw material.
A kind of process that at least one embodiment of the present invention provides, including：High level salt solution described in first aspect steams
Send out crystallizer；
Raw material enters from head tank by feed pump 1300, condenses water preheater 900 through level-one and B-grade condensation water preheats
Device 1100 enters after falling film heating room 100 is heated after heating enters the progress vapor-liquid separation of vapour liquid separator 200；By vapor-liquid separation
A part of liquid after 200 vapor-liquid separation of device is back to falling film heating room 100, another part liquid warp through primary cycle pump 1400
Punishment in advance pump 600 enters crystal separator 300, and the feed liquid from crystal separator 300 out passes through secondary cycle pump 700 and inertia
Enter forced circulation heating chamber 400 after particle mixing, entering liquid-solid separator 500 by the feed liquid after oven heats carries out liquid
Gu separation, solid phase are recycled in forced circulation heating chamber 400, into the inert particle separation in forced circulation heating chamber 400, liquid
Mutually enter crystal separator 300 and carry out vapor-liquid separation；
It should be noted that since the straight pipe out of liquid-solid separator 500 out directly goes out with secondary cycle pump 700
Expects pipe connects, but since the pressure of secondary cycle pump 700 is excessive, the phenomenon backflowed in liquid-solid separator 500 easily occurs,
So as to form accumulation, work efficiency is have impact on, in order to solve above-mentioned reflux problem, the straight tube in liquid-solid separator 500 out
Nozzle is designed with certain altitude in section, height here is determined by different operating modes, and carrying out constriction by nozzle adds
Backflow into the resistance of liquid-solid separator 500；Furthermore it is also possible to select alternative solution of the elbow as nozzle, elbow is arranged on
Straight pipe in liquid-solid separator 500 out, and bend pipe opening is consistent with Flow of Goods and Materials direction, and bend pipe also has certain neck
Contracting, so as to reach the problem of preventing from backflowing.
After raw material carries out vapor-liquid separation in vapour liquid separator 200 and crystal separator 300, indirect steam is mixed into one
Level compressor 800 is compressed, and steam after compression is partly into falling film heating room 100 and is used as heat source, generation
Condensed water preheats raw material through level-one condensation water preheater 900, and another part is further pressed into split-compressor 1000
Contracting, compressed steam is used as heat source into forced circulation heating chamber 400 again, and the condensed water of generation is through B-grade condensation water
Preheater 1100 preheats raw material.
The high level salt solution evaporation crystallization equipment that at least one embodiment of the present invention provides, the performance phase with existing compressor
Than reply boiling point rises the material more than 15 DEG C, using MVR evaporation processes, it is not necessary to more compressors of connecting, due to compressor
Energy consumption increases as admission pressure increases, therefore so that the energy consumption of whole system reduces；Increase in the raw material being evaporated
Add inert particle and make it that impurity content is more in script waste water, evaporation process easily forms fouling, the problem of influencing to conduct heat
It is resolved, because adding the raw material of inert particle because flow-disturbing and collision are so that structure greatly reduces, week is cleaned in extension
Phase.Relative to existing common total head series connection MVR, energy consumption is low, small investment.
The high level salt solution evaporation crystallization equipment and process of the present invention are illustrated above, still, the present invention is not
Above-mentioned specific embodiment is defined in, without departing from the scope of claim, various deformations or change can be carried out
More.The invention includes various changes and modifications within the scope of the claims.
Finally it should be noted that：The above embodiments are only used to illustrate the technical solution of the present invention., rather than its limitations；To the greatest extent
Pipe is described in detail the present invention with reference to foregoing embodiments, it will be understood by those of ordinary skill in the art that：Its according to
Can so modify to the technical solution described in foregoing embodiments, either to which part or all technical characteristic into
Row equivalent substitution；And these modifications or replacement, the essence of appropriate technical solution is departed from various embodiments of the present invention technology
The scope of scheme.
Claims (10)
- A kind of 1. high level salt solution evaporation crystallization equipment, it is characterised in that including：Falling film heating room (100), vapour liquid separator (200), crystal separator (300), forced circulation heating chamber (400) and liquid-solid separator (500)；The falling film heating room (100) for heating raw material is equipped with falling film heating room liquid outlet opening (110), and the falling liquid film adds Hot cell liquid outlet opening (110) is connected with the vapour liquid separator liquid inlet opening (210) of the vapour liquid separator (200)；The vapour liquid separator (200) for vapor-liquid separation is equipped with the first liquid outlet opening of vapour liquid separator (220), from described A part of liquid that vapour liquid separator (200) comes out passes through described in first liquid outlet opening of vapour liquid separator (220) entrance Crystal separator (300)；Crystal separator circulation discharge port (310) is provided with the crystal separator (300), the crystal separator recycles Material mouth (310) is connected with the forced circulation heating chamber (400)；Feed liquid after being heated by the forced circulation heating chamber (400), which enters, carries out solid-liquid in the liquid-solid separator (500) Separation；Solid phase is recycled into the forced circulation heating chamber in liquid by the liquid-solid separator (500) separation of solid and liquid (400)；Liquid phase enters the crystal separator (300) in liquid by the liquid-solid separator (500) separation of solid and liquid；Described Vapor-liquid separation is carried out in crystal separator (300), is discharged after crystal grain crystallization.
- 2. high level salt solution evaporation crystallization equipment according to claim 1, it is characterised in that add into the forced circulation Inert particle is added with before hot cell (400), the inert particle is consolidated in the forced circulation heating chamber (400) and the liquid Separator is circulated between (500).
- 3. high level salt solution evaporation crystallization equipment according to claim 2, it is characterised in that the inert particle for not with original Expect the material reacted.
- 4. high level salt solution evaporation crystallization equipment according to claim 1, it is characterised in that in the vapour liquid separator first Liquid outlet opening (220), which enters on the circulation passage of the crystal separator (300), is provided with punishment in advance pump (600).
- 5. high level salt solution evaporation crystallization equipment according to claim 1, it is characterised in that the crystal separator recycles Material mouth (310) pumps (700) by secondary cycle with the forced circulation heating chamber (400) and is connected.
- 6. high level salt solution evaporation crystallization equipment according to claim 1, it is characterised in that from the vapour liquid separator (200) another part liquid out is back to the falling film heating room by vapour liquid separator second liquid discharge port (230) (100)。
- 7. high level salt solution evaporation crystallization equipment according to claim 1, it is characterised in that the vapour liquid separator (200) After carrying out vapor-liquid separation with the crystal separator (300), the vapour liquid separator (200) top is provided with vapour liquid separator Steam (vapor) outlet (240), crystal separator steam (vapor) outlet (320) is provided with the crystal separator (300) top；After the steam mixing that the vapour liquid separator steam (vapor) outlet (240) and the crystal separator steam (vapor) outlet (320) come out It is compressed into stage compressor (800), compressed a part of steam enters the falling film heating room (100).
- 8. high level salt solution evaporation crystallization equipment according to claim 1, it is characterised in that in the falling film heating room (100) lower part is provided with falling film heating room condensation-water drain (120), is flowed from falling film heating room condensation-water drain (120) The condensed water gone out condenses water preheater (900) by level-one and raw material is heated.
- 9. high level salt solution evaporation crystallization equipment according to claim 7, it is characterised in that in the vapour liquid separator steam Enter stage compressor (800) progress after exporting the steam mixing of (240) and the crystal separator steam (vapor) outlet (320) out Compression, compressed another part steam are heated by split-compressor (1000) compressed steam into the forced circulation Room (400).
- A kind of 10. process, it is characterised in that including：Claim 1-9 any one of them high level salt solution evaporative crystallizations Equipment；Raw material enters from head tank (1200) by feed pump (1300), through level-one condensation water preheater (900) and B-grade condensation Enter vapour liquid separator (200) progress vapor-liquid separation after entering falling film heating room (100) heating after water preheater (1100) heating； A part of liquid after vapour liquid separator (200) vapor-liquid separation pumps (1400) through primary cycle and is back to falling film heating room (100), another part liquid pumps (600) through punishment in advance and enters crystal separator (300), from crystal separator (300) out Feed liquid is pumped by secondary cycle enters forced circulation heating chamber (400) after (700) are mixed with inert particle, by forced circulation plus Feed liquid after the heating of hot cell (400) enters liquid-solid separator (500) and carries out solid-liquor separation, and solid phase is recycled to forced circulation heating chamber (400) in, into the inert particle separation in forced circulation heating chamber (400), liquid phase enters crystal separator (300) and carries out vapour Liquid separates；After raw material carries out vapor-liquid separation in vapour liquid separator (200) and crystal separator (300), indirect steam is mixed into one Level compressor (800) is compressed, and steam after compression is partly into falling film heating room (100) and be used as heat source, production Raw condensed water preheats raw material through level-one condensation water preheater (900), and another part enters split-compressor (1000) Further compress, compressed steam is used as heat source, the condensed water warp of generation into forced circulation heating chamber (400) again B-grade condensation water preheater (1100) preheats raw material.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108686393A (en) * | 2018-07-15 | 2018-10-23 | 湖北开元化工科技股份有限公司 | Concentration technology in ammonium sulfate waste water MVR evaporation and crystallization system processing procedures |
| CN109091905A (en) * | 2018-09-13 | 2018-12-28 | 四川龙蟒钛业股份有限公司 | Sulfuric acid method titanium pigment vacuum crystallization system and method |
| CN109734117A (en) * | 2018-12-20 | 2019-05-10 | 聊城市鲁西化工工程设计有限责任公司 | A kind of technique of the useless calcium chloride solution cycling and reutilization containing organic matter |
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| CN107913526B (en) | 2023-09-12 |
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